Mediated electrochemical oxidation used for sterilization/disinfection

ABSTRACT

A medicated electrochemical oxidation process is used for sterilization/disinfection of contaminated instruments and infectious waste. Contaminated instruments and waste are introduced into an apparatus for contacting the infectious waste with an electrolyte containing the oxidized form of one or more reversible redox couples, at least one of which is produced at the anode of an electrochemical cell. The oxidized species of the redox couples oxidize the infectious waste molecules and are themselves converted to their reduced form, whereupon they are reoxidized by either of the aforementioned mechanisms and the redox cycle continues until all oxidizable infectious waste species have undergone the desired degree of oxidation. The entire process takes place at temperatures between ambient and approximately 100 degree celsius. The oxidation process will be enhanced by the addition of reaction of reaction enhancements, such as: ultrasonic energy and/or ultraviolet radiation.

FIELD OF THE INVENTION

This invention relates generally to a process and apparatus for using mediated electrochemical oxidation (MEO) for sterilization and/or disinfection of instruments, equipment, glassware, utensils, and materials which includes, but is not limited to, medical waste, infectious waste, pathological waste, animal waste, and combined waste (e.g. a mixture of any of the foregoing with each other or other non-biological waste) henceforth collectively referred to as infectious waste. Sterilization is the destruction of all infectious agents from an environment which includes, but not limited to, algae, bacteria, fungi, protozoa, virus dormant endospores, poorly characterized agents such as viroids and the agents that are associated with sporgiforms. Disinfection is the removal from an environment of microbes that may cause disease.

The following documents are added to the definition so as to further clarify the scope and definition of sterilization/disinfection that is considered by any of, but not limited to, the following statutes and regulations:

-   -   New Jersey State Statute, “Comprehensive Regulatory Medical         Waste Management Act”, P.L. 1989, c. 34 (C.13.1E-48.13).     -   New York State Environmental Conservation Law, TITLE 15,         “STORAGE, TREATMENT, DISPOSAL AND TRANSPORTATION OF REGULATED         MEDICAL WASTE”, Section 27-1501. Definitions.     -   New York State Public Health Law, TITLE XIII, “STORAGE,         TREATMENT AND DISPOSAL OF REGULATED MEDICAL WASTE”, Section         1389-aa. Definitions.     -   CALIFORNIA HEALTH AND SAFETY CODE, SECTION 117635. “Biohazardous         Waste” Title 25 Health Services, Part I.     -   Texas Department of Health, Chapter 1 Texas Board of Health,         “Definition, Treatment, and Disposition of Special Waste from         Health Care-Related Facilities, Section 1.132 Definitions.     -   40 C.F.R. 60.51 (c) PROTECTION OF ENVIRONMENT; Standards of         performance for new stationary sources.     -   40 C.F.R. 240.101 PROTECTION OF ENVIRONMENT; Guidelines for the         thermal processing of solid wastes (Section P only).     -   49 C.F.R. 173.134 TRANSPORTATION; Class 6, Division         6.2-Definitions, exceptions and packing group assignments.     -   33 C.F.R. 151.05 TITLE 33 □□NAVIGATION AND NAVIGABLE WATERS;         VESSELS CARRYING OIL, NOXIOUS LIQUID SUBSTANCES, GARBAGE,         MUNICIPAL OR COMMERCIAL WASTE, AND BALLAST WATER□; Definitions         (medical waste only).

The definition of infectious waste has been expanding in its coverage of materials that must be handled in a controlled manner. The foregoing list of State statutes and United States Federal Regulations are overlapping but are necessary to accurately define the materials since no single statute or regulation covers all the materials for which this invention applies.

BACKGROUND OF THE INVENTION

The cost of sterilization/disinfection in the U.S. is a multi-billion dollar per year industry. The capital cost of the sterilization/disinfection equipment and/or the chemicals used in sterilization/disinfection is in the hundreds of millions of dollars. All institutions and businesses that generate and handle this category of infectious waste must provide safe effective and inexpensive disposal of the infectious waste. In recent years there has been increasing concern over the disposal of infectious waste. The two principle methodologies for the disposal of this infectious waste are by (a) physical methods such as steam or dry heat, UV lamps, infrared radiation, microwaves, gamma radiation and membrane filtration; and (b) chemical sterilants and disinfectants such as halogen compounds, non-halogen chemical germicides (i.e., alcohols, phenolic compounds, quaternary ammonium compounds, hydrogen peroxide, aldehydes, and ethylene oxide gas).

The physical methods that involve heat and/or pressure systems have the following problems: a) maintenance and quality control, b) packing is critical to performance, c) time consuming, d) potential volatile hazardous organic emissions, and some equipment is heat sensitive. In the case of the use of incinerators there is the problem of transportation and the emissions of volatile hazardous organics.

Disinfectants may be effective against bacteria but not against viruses or fungi. There are differences in effectiveness between gram-positive and gram-negative bacteria and sometimes even between strains of the same species. Bacterial spores are more resistant then the vegetative form. Disinfectants have differing effects on various types of viruses such as those with lipid coatings compared to non-enveloped, non-lipid-contained viruses. Since no one chemical sterilants or disinfectants is effective for all sterilization or disinfection purposes there is a significant need for improved methods of handling infectious wastes.

The MEO process in this patent provides an apparatus and process that destroys all microbial materials on instruments, equipment, glassware, utensils, and materials at the facility that generates the infectious waste in an environment of ambient atmospheric pressure and at temperatures less then 100° C. The MEO process sterilizes and/or disinfects medical and veterinary instruments, equipment, glassware, utensils, and materials so that they can be used again. In the case of equipment that cannot stand heat or is in anyway not suitable for common sterilization techniques such as dialyzers, the MEO process and apparatus offer a new and unique approach to sterilization and/or disinfection.

SUMMARY OF THE INVENTION

The invention relates to a method and apparatus for the use of mediated electrochemical oxidation (MEO) for the sterilizing and/or disinfecting of contaminated instruments, equipment, glassware, utensils, and materials which includes, but is not limited to, medical waste, infectious waste, pathological waste, animal waste, and combined waste (e.g., a mixture of any of the foregoing with each other or other non-infectious waste) henceforth collectively referred to as infectious waste. Sterilization is the destruction of all forms of microbial life from an environment which includes, but not limited to, algae, bacteria, fungi, protozoa, virus dormant endospores, poorly characterized agents such as viroids and the agents that are associated with spongiforms. Disinfection is the removal from an environment of specific pathogenic microorganisms.

The MEO process is applied to perform sterilization and/or disinfection of instruments, equipment, glassware, utensils, and materials. The microorganisms (infectious waste) contaminate the instruments, equipment, glassware, utensils, and materials when they are used to perform functions in connection with providing medical care, veterinary care, processing food, and agricultural activities such as raising animals and plants. The MEO process sterilizes and/or disinfects medical and veterinary instruments, equipment, glassware, utensils, and materials so that they can be used again. In the case of equipment that cannot stand heat or is in anyway not suitable for common sterilization techniques such as dialyzers, the MEO process and apparatus offer a new and unique approach to sterilization and/or disinfection.

The mediated electrochemical oxidation process involves an electrolyte containing one or more redox couples, wherein the oxidized form of at least one redox couple is produced by anodic oxidation at the anode of an electrochemical cell. The oxidized forms of any other redox couples present are produced either by similar anodic oxidation or reaction with the oxidized form of other redox couples present capable of affecting the required redox reaction. The oxidized species of the redox couples oxidize the infectious waste molecules and are themselves converted to their reduced form, whereupon they are reoxidized by either of the aforementioned mechanisms and the redox cycle continues until all oxidizable infectious waste species, including intermediate reaction products, have undergone the desired degree of oxidation. The MEO process continues until the degree of sterilization/disinfection desired is accomplished. The redox species ions are thus seen to “mediate” the transfer of electrons from the infectious material to the anode, (i.e., oxidation of the all infectious waste).

A membrane in the electrochemical cell separates the anolyte and catholyte, thereby preventing parasitic reduction of the oxidizing species at the cathode. The preferred MEO process uses the mediator species described in Table I (simple anions redox couple mediators); the Type I isopolyanions (IPA) formed by Mo, W, V, Nb, and Ta, and mixtures there of; the Type I heteropolyanions (HPA) formed by incorporation into the aforementioned isopolyanions of any of the elements listed in Table II (heteroatoms) either singly or in combinations there of; any type heteropolyanion containing at least one heteropolyatom (i.e. element) contained in both Table I and Table II; or combinations of mediator species from any or all of these generic groups.

Simple Anion Redox Couple Mediators

Table I shows the simple anion redox couple mediators used in the preferred MEO process wherein “species” defines the specific ions for each chemical element that have applicability to the MEO process as either the reduced (e.g., Fe⁺³) or oxidizer (e.g., FeO₄ ⁻²) form of the mediator characteristic element (e.g., Fe), and the “specific redox couple” defines the specific associations of the reduced and oxidized forms of these species (e.g., Fe⁺²/FeO₄ ⁻²) that are claimed for the MEO process. Species soluble in the anolyte are shown in Table I in normal print while those that are insoluble are shown in bold underlined print. The characteristics of the MEO Process claimed in this patent are specified in the following paragraphs.

The anolyte contains one or more redox couples which in their oxidized form consist of either single multivalent element anions (e.g., Ag⁺², Ce⁺⁴, Co⁺³, Pb⁺⁴, etc.), insoluble oxides of multivalent elements (e.g., PbO₂, CeO₂, PrO₂, etc.), or simple oxoanions (also called oxyanions) of multivalent elements (e.g., FeO₄ ⁻², NiO₄ ⁻², BiO₃ ⁻, etc.) called the mediator species. The nonoxygen multivalent element component of the mediator is called the characteristic element of the mediator species. We have chosen to group the simple oxoanions with the simple anion redox couple mediators rather than with the complex (i.e., polyoxometallate (POM)) anion redox couple mediators discussed in the next section and refer to them collectively as simple anion redox couple mediators.

In one embodiment of this process both the oxidized and reduced forms of the redox couple are soluble in the anolyte. The reduced form of the couple is anodically oxidized to the oxidized form at the cell anode(s) whereupon it oxidizes molecules of infectious waste either dissolved in or located on infectious waste particle surfaces wetted by the anolyte, with the concomitant reduction of the oxidizing agent to its reduced form, whereupon the MEO process begins again with the reoxidation of this species at the cell anode(s). If other less powerful redox couples of this type (i.e., reduced and oxidized forms soluble in anolyte) are present, they too may undergo direct anodic oxidation or the anodically oxidized more powerful oxidizing agent may oxidize them rather that a infectious waste molecule. The weaker redox couple(s) is selected such that their oxidation potential is sufficient to affect the desired reaction with the infectious waste molecules. The oxidized species of all the redox couples oxidize the infectious waste materials and are themselves converted to their reduced form, whereupon they are reoxidized by either of the aforementioned mechanisms and the redox cycle continues until all oxidizable infectious waste species, including intermediate reaction products, have undergone the desired degree of oxidation.

The preferred mode for the MEO process as described in the preceding section is for the redox couple species to be soluble in the anolyte in both the oxidized and reduced forms; however this is not the only mode of operation claimed herein. If the reduced form of the redox couple is soluble in the anolyte (e.g., Pb⁺²) but the oxidized form is not (e.g., PbO₂), the following processes are operative. The insoluble oxidizing agent is produced either as a surface layer on the anode by anodic oxidation, or throughout the bulk of the anolyte by reacting with the oxidized form of other redox couples present capable of affecting the required redox reaction, at least one of which is formed by anodic oxidation. The oxidizable infectious waste is either soluble in the anolyte or dispersed therein as a fine particle size, (e.g., emulsion, colloid, etc.) thereby affecting intimate contact with the surface of the insoluble oxidizing agent (e.g., PbO₂) particles. Upon reaction of the infectious waste with the oxidizing agent particles, the infectious waste is oxidized and the insoluble oxidizing agent molecules on the anolyte wetted surfaces of the oxidizing agent particles reacting with the infectious waste are reduced to their soluble form and are returned to the bulk anolyte, available for continuing the MEO process by being reoxidized.

In another variant of the MEO process if the reduced form of the redox couple is insoluble in the anolyte (e.g., TiO₂) but the oxidized form is soluble (e.g., TiO₂ ⁺²), the following processes are operative. The soluble (i.e., oxidized) form of the redox couple is produced by the reaction of the insoluble (i.e., reduced form) redox couple molecules on the anolyte wetted surfaces of the oxidizing agent particles with the soluble oxidized form of other redox couples present capable of affecting the required redox reaction, at least one of which is formed by anodic oxidation and soluble in the anolyte in both the reduced and oxidized forms. The soluble oxidized species so formed are released into the anolyte whereupon they oxidize infectious waste molecules in the manner previously described and are themselves converted to the insoluble form of the redox couple, thereupon returning to the starting point of the redox MEO cycle.

The electrolytes used in this claim are from a family of acids, alkali, and neutral salt aqueous solutions (e.g. sulfuric acid, potassium hydroxide, sodium sulfate aqueous solutions etc.).

A given redox couple or mixture of redox couples (i.e. mediator species) will be used with different electrolytes.

The electrolyte composition is selected based on demonstrated adequate solubility of the compound containing at least one of the mediator species present in the reduced form (e.g., sulfuric acid will be used with ferric sulfate, etc.).

The concentration of the mediator species containing compounds in the anolyte will range from 0.0005 molar (M) up to the saturation point.

The concentration of electrolyte in the anolyte will be governed by its effect upon the solubility of the mediator species containing compounds and by the conductivity of the anolyte solution desired in the electrochemical cell for the given mediator species being used.

The temperature over which the electrochemical cell will be operated will range from approximately 0° C. to slightly below the boiling point of the electrolytic solution.

The MEO process is operating at atmospheric pressure.

The mediator species are differentiated on the basis of whether they are capable of reacting with the electrolyte to produce free radicals (e.g., •O₂H (perhydroxyl), •OH (hydroxyl), •SO₄ (sulfate), •NO₃ (nitrate), etc.). Such mediator species are classified herein as “super oxidizers” (SO) and typically exhibit oxidation potentials at least equal to that of the Ce⁺³/Ce⁺⁴ redox couple (i.e., 1.7 volts).

The electrical potential between the electrodes in the electrochemical cell is based upon the oxidation potential of the most reactive redox couple present in the anolyte and serving as a mediator species, and the ohmic losses within the cell. Within the current density range of interest the electrical potential will be approximately 2.5 to 3.0 volts.

Complex Anion Redox Couple Mediators

The preferred characteristic of the oxidizing species in the MEO process is that it be soluble in the aqueous anolyte in both the oxidized and reduced states. The majorities of metal oxides and oxoanion (oxyanion) salts are insoluble, or have poorly defined or limited solution chemistry. The early transition elements, however, are capable of spontaneously forming a class of discrete polymeric structures called POMs (POMs) which are highly soluble in aqueous solutions over a wide pH range. The polymerization of simple tetrahedral oxoanions of interest herein involves an expansion of the metal, M, coordination number to 6, and the edge and corner linkage of MO₆ octahedra. Chromium is limited to a coordination number of 4, restricting the POMs based on CrO₄ tetrahedra to the dichromate ion [Cr₂O₇]⁻² which is included in Table I. Based upon their chemical composition POMs are divided into the two subclasses isopolyanions (IPAs) and heteropolyanions (HPAs), as shown by the following general formulas: Isopolyanions (IPAs)—[M_(m)O_(y)]^(p−) and, Heteropolyanions (HPAs)—[X_(x)M_(m)O_(y)]^(q−)(m>x) where the addenda atom, M, is usually Molybdenum (Mo) or Tungsten (W), and less frequently Vanadium (V), Niobium (Nb), or Tantalum (Ta), or mixtures of these elements in their highest (d⁰) oxidation state. The elements that can function as addenda atoms in IPAs and HPAs appear to be limited to those with both a favorable combination of ionic radius and charge, and the ability to form dn-pn M—O bonds. However, the heteroatom, X, have no such limitations and can be any of the elements listed in Table II.

There is a vast chemistry of POMs that involves the oxidation/reduction of the addenda atoms and those heteroatoms listed in Table II, which exhibit multiple oxidation states. The partial reduction of the addenda, M, atoms in some POMs strictures (i.e., both IPAs and HPAs) produces intensely colored species, generically referred to as “heteropoly blues”. Based on structural differences, POMs can be divided into two groups, Type I and Type II. Type I POMs consist of MO₆ octahedra each having one terminal oxo oxygen atom while Type II have 2 terminal oxo oxygen atoms. Type II POMs can only accommodate addenda atoms with d⁰ electronic configurations, whereas Type I; e.g., Keggin (XM₁₂O₄₀), Dawson (X₂M₁₈O₆₂), hexametalate (M₆O₁₉), decatungstate (W₁₀O₃₂), etc., can accommodate addenda atoms with d⁰, d¹, and d² electronic configurations. Therefore, while Type I structures can easily undergo reversible redox reactions, structural limitations preclude this ability in Type II structures. Oxidizing species applicable for the MEO process are therefore Type I POMs (i.e., IPAs and HPAs) where the addenda, M, atoms are W, Mo, V, Nb, Ta, or combinations thereof.

The high negative charges of polyanions often stabilize heteroatoms in unusually high oxidation states, thereby creating a second category of MEO oxidizers in addition to the aforementioned Type I POMs. Any Type I or Type II HPA containing any of the heteroatom elements, X, listed in Table II, that also are listed in Table I as simple anion redox couple mediators, can also function as an oxidizing species in the MEO process.

The anolyte contains one or more complex anion redox couples, each consisting of either the afore mentioned Type I POMs containing W, Mo, V, Nb, Ta or combinations there of as the addenda atoms, or HPAs having as heteroatoms (X) any elements contained in both Tables I and II, and which are soluble in the electrolyte (e.g. sulfuric acid, etc.).

The electrolytes used in this claim are from a family of acids, alkali, and neutral salt aqueous solutions (e.g. sulfuric acid, potassium hydroxide, sodium sulfate aqueous solutions, etc.).

A given POM redox couple or mixture of POM redox couples (i.e., mediator species) will be used with different electrolytes.

The electrolyte composition is selected based on demonstrating adequate solubility of at least one of the compounds containing the POM mediator species in the reduced form and being part of a redox couple of sufficient oxidation potential to affect oxidation of the other mediator species present.

The concentration of the POM mediator species containing compounds in the anolyte will range from 0.0005M up to the saturation point. The concentration of electrolyte in the anolyte will be governed by its effect upon the solubility of the POM mediator species containing compounds and by the conductivity of the anolyte solution desired in the electrochemical cell for the given POM mediator species being used to allow the desired cell current at the desired cell voltage.

The temperature over which the electrochemical cell will be operated will range from approximately 0° C. to just below the boiling point of the electrolytic solution.

The MEO process is operating at atmospheric pressure.

The POM mediator species are differentiated on the basis of whether they are capable of reacting with the electrolyte to produce free radicals (e.g., •O₂H, •OH , •SO₄, •NO₃) Such mediator species are classified herein as “super oxidizers” (SO) and typically exhibit oxidation potentials at least equal to that of the Ce⁺³/Ce⁺⁴ redox couple (i.e., 1.7 volts).

The electrical potential between the electrodes in the electrochemical cell is based on the oxidation potential of the most reactive POM redox couple present in the anolyte and serving as a mediator species, and the ohmic losses within the cell. Within the current density range of interest the electrical potential will be approximately 2.5 to 3.0 volts.

Mixed Simple and Complex Anion Redox Couple Mediators

The preferred MEO process for a combination of simple and complex anion redox couple mediators may be mixed together to form the system anolyte. The characteristics of the resulting MEO process is similar to the previous discussions.

The use of multiple oxidizer species in the MEO process has the following potential advantages:

-   -   a) The overall infectious waste destruction rate will be         increased if the reaction kinetics of anodically oxidizing         mediator “A”, oxidizing mediator “B” and oxidized mediator “B”         oxidizing the infectious waste is sufficiently rapid such that         the combined speed of the three step reaction train is faster         than the two step reaction trains of anodically oxidizing         mediator “A” or “B”, and the oxidized mediators “A” or “B”         oxidizing the infectious waste, respectively.     -   b) If the cost of mediator “B” is sufficiently less than that of         mediator “A”, the used of the above three step reaction train         will result in lowering the cost of infectious waste destruction         due to the reduced cost associated with the smaller required         inventory and process losses of the more expensive mediator “A”.         An example of this the use of a silver (II)-peroxysulfate         mediator system to reduce the cost associated with silver and         overcome the slow oxidation kinetics of peroxysulfate only MEO         process.     -   c) The MEO process is “desensitized” to changes in the types of         molecular bonds present in the infectious waste as the use of         multiple mediators, each selectively attacking different type of         chemical bonds, results in a highly “nonselective” oxidizing         system.         Anolyte Additional Features

In one preferred embodiment of the MEO process in this invention, there are one or more simple anion redox couple mediators in the anolyte aqueous solution. In a preferred embodiment of the MEO process, there are one or more complex anion (i.e., POMs) redox couple mediators in the anolyte aqueous solution. In another preferred embodiment of the MEO process, there are one or more simple anion redox couples and one or more complex anion redox couples in the anolyte aqueous solution.

The MEO process of the present invention uses any oxidizer species listed in Table I that are found in situ in the infectious waste to be destroyed; For example, when the infectious waste also contains lead compounds that become a source of Pb⁺² ions under the MEO process conditions within the anolyte, the infectious waste-anolyte mixture will be circulated through an electrochemical cell. Where the oxidized form of the reversible lead redox couple will be formed either by anodic oxidation within the electrochemical cell or alternately by reacting with the oxidized form of a more powerful redox couple, if present in the anolyte and the latter being anodically oxidized in the electrochemical cell. The lead thus functions exactly as a simple anion redox couple species thereby destroying the organic waste component leaving only the lead to be disposed of. Adding one or more of any of the anion redox couple mediators described in this patent will further enhance the MEO process described above.

In the MEO process of the invention, anion redox couple mediators in the anolyte part of an aqueous electrolyte solution will use an acid, neutral or alkaline solution depending on the temperature and solubility of the specific mediator(s). The anion oxidizers used in the basic MEO process preferably attack specific organic molecules. Hydroxyl free radicals preferentially attack organic molecules containing aromatic rings and unsaturated carbon-carbon bonds Oxidation products such as the highly undesirable aromatic compounds chlorophenol or tetrachlorodibenzodioxin (dioxin) upon formation would thus be preferentially attacked by hydroxyl free radicals, preventing the accumulation of any meaningful amounts of these compounds. Even free radicals with lower oxidation potentials than the hydroxyl free radical preferentially attack carbon-halogen bonds such as those in carbon tetrachloride and polychlorobiphenyls (PCBs).

Some redox couples having an oxidation potential at least equal to that of the Ce⁺³/Ce⁺⁴ redox couple (i.e., 1.7 volts), and sometimes requiring heating to above about 50° C. (i.e., but less then the boiling point of the electrolyte) can initiate a second oxidation process wherein the mediator ions in their oxidized form interact with the aqueous anolyte, creating secondary oxidizer free radicals (e.g., •O₂H, •OH, •SO₄, •NO₃, etc.) or hydrogen peroxide. Such mediator species in this invention are classified herein as “super oxidizers” (SO) to distinguish them from the “basic oxidizers” incapable of initiating this second oxidation process.

The oxidizer species addressed in this patent (i.e., characteristic elements having atomic number below 90) are described in Table I (simple anions redox couple mediators): Type I IPAs formed by Mo, W, V, Nb, Ta, or mixtures there of as addenda atoms; Type I HPAs formed by incorporation into the aforementioned IPAs if any of the elements listed in Table II (heteroatoms) either singly or in combinations thereof; or any HPA containing at least one heteroatom type (i.e., element) contained in both Table I and Table II; or mediator species from any or all of these generic groups.

Each oxidizer anion element has normal valence states (NVS) (i.e., reduced form of redox couple) and higher valence states (HVS) (i.e., oxidized form of redox couple) created by stripping electrons off NVS species when they pass through and electrochemical cell. The MEO process of the present invention uses a broad spectrum of anion oxidizers; these anion oxidizers used in the basic MEO process may be interchanged in the preferred embodiment without changing the equipment.

In preferred embodiments of the MEO process, the basic MEO process is modified by the introduction of additives such as tellurate or periodate ions which serve to overcome the short lifetime of the oxidized form of some redox couples (e.g., Cu⁺³) in the anolyte via the formation of more stable complexes (e.g., [Cu(IO₆)₂]⁻⁷, [Cu(HteO₆)₂]⁻⁷) The tellurate and periodate ions can also participate directly in the MEO process as they are the oxidized forms of simple anion redox couple mediators (see Table I) and will participate in the oxidation of infectious waste in the same manner as previously described for this class of oxidizing agents.

Alkaline Electrolytes

In one preferred embodiment, a cost reduction will be achieved in the basic MEO process by using an alkaline electrolyte, such as but not limited to aqueous solutions of NaOH or KOH with mediator species wherein the reduced form of said mediator redox couple displays sufficient solubility in said electrolyte to allow the desired oxidation of the infectious waste to proceed at a practical rate. The oxidation potential of redox reactions producing hydrogen ions (i.e., both mediator species and infectious waste molecules reactions) are inversely proportional to the electrolyte pH, thus with the proper selection of a redox couple mediator, it is possible, by increasing the electrolyte pH, to minimize the electric potential required to affect the desired oxidation process, thereby reducing the electric power consumed per unit mass of infectious waste destroyed.

When an alkaline anolyte (e.g., NaOH, KOH, etc.) is used, benefits are derived from the saponification (i.e., base promoted ester hydrolysis) of fatty acids to form water soluble alkali metal salts of the fatty acids (i.e., soaps) and glycerin, a process similar to the production of soap from animal fat by introducing it into a hot aqueous lye solution.

In this invention, when an alkaline anolyte is used, the CO₂ resulting from oxidation of the infectious waste reacts with the anolyte to form alkali metal bicarbonates/carbonates. The bicarbonate/carbonate ions circulate within the anolyte where they are reversibly oxidized to percarbonate ions either by anodic oxidation within the electrochemical cell or alternately by reacting with the oxidized form of a more powerful redox couple mediator, when present in the anolyte. The carbonate thus functions exactly as a simple anion redox couple mediator, thereby producing an oxidizing species from the infectious waste oxidation products that it is capable of destroying additional infectious waste.

Additional MEO Electrolyte Features

In one preferred embodiment of this invention, the catholyte and anolyte are discrete entities separated by a membrane, thus they are not constrained to share any common properties such as electrolyte concentration, composition, or pH (i.e., acid, alkali, or neutral). The process operates over the temperature range from approximately 0° C. to slightly below the boiling point of the electrolyte used during the destruction of the infectious waste.

MEO Process Augmented by Ultraviolet/Ultrasonic Energy

Decomposition of the hydrogen peroxide into free hydroxyl radicals is well known to be promoted by ultraviolet (UV) irradiation. The destruction rate of infectious waste obtained using the MEO process in this invention, will, therefore, be increased by UV irradiation of the reaction chamber anolyte to promote formation of additional hydroxyl free radicals. In a preferred embodiment, UV radiation is introduced into the anolyte chamber using a UV source either internal to or adjacent to the anolyte chamber. The UV irradiation decomposes hydrogen peroxide, which is produced by secondary oxidizers generated by the oxidized form of the mediator redox couple, into hydroxyl free radical. The result is an increase in the efficiency of the MEO process since the energy expended in hydrogen peroxide generation is recovered through the oxidation of infectious materials in the anolyte chamber.

Additionally, in a preferred embodiment, ultrasonic energy will be applied into the anolyte chamber to rupture the cell membranes and affect dispersal within the anolyte of the infectious materials. The ultrasonic energy is absorbed in the cell wall and the local temperature in the immediate vicinity of the cell wall is raised to above several thousand degrees, resulting in cell wall failure. This substantially increases the effectiveness of oxidation by MEO oxidizer species as well as the overall efficiency of the MEO process. In another embodiment, ultrasonic energy is introduced into the anolyte chamber. Implosion of the microscopic bubbles formed by the rapidly oscillating pressure waves emanating from the sonic horn generate shock waves capable of producing extremely short lived and localized conditions of 4800° C. and 1000 atmospheres pressure within the anolyte. Under these conditions water molecules decompose into hydrogen atoms and hydroxyl radicals. Upon quenching of the localized thermal spike, the hydroxyl radicals will undergo the aforementioned reactions with the infectious waste or combine with each other to form another hydrogen peroxide which will then itself oxidize additional infectious waste.

In another preferred embodiment, the destruction rate of non anolyte soluble infectious waste is enhanced by affecting a reduction in the dimensions of the individual second (i.e., infectious waste) phase entities present in the anolyte, thereby increasing the total infectious waste surface area wetted by the anolyte and therefore the amount of infectious waste oxidized per unit time. Immsicible liquids may be dispersed on an extremely fine scale within the aqueous anolyte by the introduction of suitable surfactants or emulsifying agents. Vigorous mechanical mixing such as with a colloid mill or the microscopic scale mixing affected by the aforementioned ultrasonic energy induced microscopic bubble implosion could also be used to affect the desired reduction in size of the individual second phase infectious waste volumes dispersed in the anolyte. The vast majority of tissue based infectious waste will be converted from a semi-rigid solid into a liquid phase, thus becoming treatable as above, using a variety of cell disruption methodologies. Examples of these methods are mechanical shearing using various rotor-stator homogenizers and ultrasonic devices (i.e., sonicators) where the aforementioned implosion generated shock wave, augmented by the 4800° C. temperature spike, shear the cell walls. Distributing the cell protoplasm throughout the anolyte produces an immediate reduction in the mass and volume of actual infectious wastes as about 67 percent of protoplasm is ordinary water, which simply becomes part of the aqueous anolyte, requiring no further treatment. If the amount of water released directly from the infectious waste and/or formed as a reaction product from the oxidation of hydrogenous waste dilutes the anolyte to an unacceptable level, the anolyte can easily be reconstituted by simply raising the temperature and/or lowering the pressure in an optional evaporation chamber to affect removal of the required amount of water. The soluble constituents of the protoplasm are rapidly dispersed throughout the anolyte on a molecular scale while the insoluble constituents will be dispersed throughout the anolyte as an extremely fine second phase using any of the aforementioned dispersal methodologies, thereby vastly increasing the infectious waste anolyte interfacial contact area beyond that possible with an intact cell configuration and thus the rate at which the infectious waste is destroyed and the MEO efficiency.

MEO Process Augmented with Free Radicals

The principals of the oxidation process used in this invention in which a free radical (e.g., O₂H, OH, SO₄, NO₃,) will cleave and oxidize organic compounds resulting in the formation of successively smaller chained hydrocarbon compounds. The intermediate compounds formed are easily oxidized to carbon dioxide and water during sequential reactions.

Inorganic radicals will be generated in aqueous solutions variants of the MEO process in this invention. Radicals have been derived from carbonate, azide, nitrite, nitrate, phosphate, phosphite, sulphite, sulphate, selenite, thiocyanate, chloride, bromide, iodide and formate ions. Organic free radicals, such as sulfhydryl, will be generated using the basic MEO process. When the MEO process in this invention is applied to infectious materials they break down the materials into organic compounds that are attacked by the aforementioned inorganic free radicals. The inorganic free radicals produce organic free radicals, which contribute to the oxidation process and increase the efficiency of the MEO process.

MEO Process for Sharps

A preferred embodiment of the MEO process used in this invention generates the perbromate ion as the oxidizing mediator species will be used to destroy stainless steel products such as sharps, which include but are not limited to syringe needles, scalpels, and sutures.

SUMMARY

These and further and other objects and features of the invention are apparent in the disclosure, which includes the above and ongoing written specification, with the claims and drawings.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1A MEO Apparatus Diagram is a schematic representation of a system for sterilizing and disinfecting instruments, equipment, glassware, utensils, and materials by destroying infectious waste materials. FIG. 1A is a representation of a general embodiment of the present invention (with the understanding that not all of the components shown therein must necessarily be employed in all situations).

FIG. 1B Anolyte Reaction Chamber for Sterilization is a schematic representation of the anolyte reaction chamber used for sterilization of infectious waste contaminated instruments, equipment, glassware, utensils, and materials. The system depicted in this figure is similar in design to a laboratory glassware washer where the fluid in the wash is the anolyte.

FIG. 1C Anolyte Reaction Chamber for Disinfection is a schematic representation of the anolyte reaction chamber used to disinfect infectious waste contaminated instruments, equipment, glassware, utensils, and materials.

FIG. 1D Remote Anolyte Reaction Chamber (Sterilization) is a schematic representation of the anolyte reaction chamber used for separating the anolyte reaction chamber from the basic MEO apparatus. This configuration allows the chamber to be a part of a primary room, such as an operatorium, laboratory or similar use, minimizing the exposure of the operating technician to the activities in the primary room.

FIG. 1E Anolyte Reaction Chamber Exterior is a schematic representation of a container serving the role of the anolyte reaction chamber that is not a part of the MEO apparatus. Typical of the exterior chamber is a dialysis system used to treat body fluids from patients suffering from kidney problems. The dialysis system is connected to the patient and circulates the patient's blood through the system to clean out body products normally removed by the kidneys. The internal tubing of the dialysis system becomes contaminated with the patient's body fluid. The MEO process thoroughly cleans and sterilizes all the contamination internal to the dialysis system between uses.

FIG. 2 MEO System Model 5.b is a schematic representation of a typical preferred embodiment. The Model 5.b uses the anolyte reaction chamber 5 a (FIG. 1B) in the MEO apparatus depicted in FIG. 1A. This model is used for the sterilization of infectious waste contaminated instruments, equipment, glassware, utensils, and materials.

FIG. 3 MEO Controller is a schematic representation of the MEO electrical and electronic systems. FIG. 3 is a representation of a general embodiment of a controller for the present invention (with the understanding that not all of the components shown therein must necessarily be employed in all situations). FIG. 3 is used to illustrate the functions of a controller by using the anolyte reaction chamber in FIG. 1B and the overall MEO system in FIG. 1A.

FIG. 4 MEO Operating Process is a schematic representation of the generalized steps of the process used in the MEO apparatus (with the understanding that not all of the components shown therein must necessarily be employed in a;; situations). FIG. 4 is used to illustrate the operating process by using the anolyte reaction chamber 5 a in FIG. 1B and the overall MEO system in FIG. 1A.

DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS

According to this present patent, the Mediated Electrochemical Oxidation (MEO) process and apparatus may oxidize infectious agents by the interaction of the oxidized species of the redox couple with the agents. The infectious agents give up at least one electron to the oxidized species of the redox couple resulting in the inactivation of the microorganism. The MEO process continues oxidizing the infectious materials on instruments, equipment, glassware, utensils, and materials until they are decomposed into carbon dioxide and water. The MEO process will accomplish sterilization on instruments, equipment, glassware, utensils, and materials by operating the apparatus until no biological material remain. When disinfection is the desired result, the MEO process may be operated a predetermined time to render the pathogenic microorganisms inactivated on all of the instruments, equipment, glassware, utensils, and materials.

MEO Chemistry

Mediated Electrochemical Oxidation (MEO) process chemistry described in this patent uses oxidizer species (i.e., characteristic elements having atomic number below 90) as described in Table I (simple anions redox couple mediators); Type I IPAs formed by Mo, W, V, Nb, Ta, or mixtures there of as addenda atoms; Type I HPAs formed by incorporation into the aforementioned IPAs of any of the elements listed in Table II (heteroatoms) either singly or in combination there of; or any HPA containing at least one heteroatom type (i.e., element) contained in both Table I and Table II; or combinations of mediator species from any or all of these generic groups. Since the anolyte and catholyte are completely separated entities, it is not necessary for both systems to contain the same electrolyte. Each electrolyte may, independent of the other, consist of an aqueous solution of acids, typically but not limited to nitric, sulfuric, of phosphoric; alkali, typically but not limited to sodium or potassium hydroxide; or neutral salt typically but not limited to sodium or potassium salts of the aforementioned strong mineral acids.

The MEO Apparatus is unique in that it accommodates the numerous choices of mediator ions and electrolytes by simply draining, flushing, and refilling the system with the mediator/electrolyte system of choice.

Because of redundancy and similarity in the description of the various mediator ions, only the iron and nitric acid combination is discussed in detail. However, it is to be understood that the following discussion of the ferric/ferrate, (Fe⁺³)/(FeO₄ ⁻²) redox couple reaction in nitric acid (HNO₃) also applies to all the aforementioned oxidizer species and electrolytes described at the beginning of this section. Furthermore, the following discussions of the interaction of ferrate ions with aqueous electrolytes to produce the aforementioned free radicals also applies to all aforementioned mediators having an oxidation potential sufficient to be classified superoxidizers, typically at least equal to that of the Ce⁺³/Ce⁺⁴ redox couple (i.e., 1.7 volts).

FIG. 1A shows a MEO Apparatus in a schematic representation for destroying infectious waste on instruments, equipment, glassware, utensils, and materials. At the anode of the electrochemical cell 25 Fe(III) ions (Fe⁺³, ferric) are oxidized to Fe(VI) ions (FeO₄ ⁻², ferrate), Fe⁺³+4H₂O→FeO⁻²+8H⁺+3e⁻

If the anolyte temperature is sufficiently high, typically above 50° C., the Fe(VI) species may undergo a redox reaction with the water in the aqueous anolyte. The oxidation of water proceeds by a sequence of reactions producing a variety of intermediate reaction products, some of which react with each other. A few of these intermediate reaction products are highly reactive free radicals including, but not limited to the hydroxyl (•OH) and hydrogen peroxy or perhydroxyl (•HO₂) radicals. Additionally, the mediated oxidizer species ions may interact with anions present in the acid or neutral salt electrolyte (e.g., NO₃ ⁻, SO₄ ⁻², or PO₄ ⁻³, etc.) to produce free radicals typified by, but not limited to •NO₃, or the anions may undergo direct oxidation at the anode of the cell. The population of hydroxyl free radicals may be increased by ultraviolet irradiation of the anolyte (see ultraviolet source 11) in the reaction chamber(s) 5(a,b,c,d) to cleave the hydrogen peroxide molecules, intermediate reaction products, into two such radicals. Free radical populations will also be increased by ultrasonic vibration (see ultrasonic source 9) induced by the aforementioned implosion generated shock wave, augmented by the 4800° C. temperature spike and 1000 atmospheres pressure.

These secondary oxidation species are capable of oxidizing organic materials and thus act in consort with Fe(VI) ions to oxidize the infectious waste on the instruments, equipment, glassware, utensils, and materials.

The oxidizers react with the infectious waste to produce CO₂ and water. These processes occur in the anolyte on the anode side of the system in the reaction chamber(s) 5(a,b,c,d). Addition of ferric ions to non-iron-based MEO systems are also proposed as this has the potential for increasing the overall rate of infectious waste oxidation compared to the non-iron MEO system alone. (Again it is to be understood this discussion of the ferric/ferrate redox couple also applies to all the aforementioned oxidizer species described at the beginning of this section.) If the two step process of electrochemically forming a FeO₄ ⁻² ion and the FeO₄ ⁻² ion oxidizing the mediator ion to its higher valance occurs faster than the direct electrochemical oxidation of the mediator ion itself, then there is an overall increase in the rate of infectious waste destruction.

Membrane 27 separates the anode and the cathode chambers in the electrochemical cell 25. Hydrogen ions (H⁺) or hydronium ions (H₃O⁺) travel through the membrane 27 due to the electrical potential from the dc power supply 29 applied between the anode(s) and cathodes(s) 26 and 28, respectively. In the catholyte the nitric acid is reduced to nitrous acid 3HNO₃+6H⁺+6e⁻→3HNO₂+H₂O by the reaction between the H⁺ ions and the nitric acid. Oxygen is introduced into the catholyte through the air sparge 37 located below the liquid surface, and the nitric acid is regenerated, 3HNO₂+3/2O₂→3HNO₃

The overall process results in the infectious waste being converted to carbon dioxide, water, and a small amount of inorganic compounds in solution or as a precipitate, which will be extracted by the inorganic compound removal and treatment system 15.

The MEO process has been tested using a whole small animal (dead) mouse. After the MEO process had run for a suitable time the physical structure of the mouse was totally converted into a liquid. The liquid was tested and only a very small amount of total carbon content was detected. The carbon content of the largest detected hydrocarbon molecules was less then ten (10) carbons per molecule. This result supports the conclusion that the contents of the liquid were sterilized and disinfected. The microorganism tests to determine the existence of microorganism will be completed following accepted protocols to substantiate the conclusion that the MEO process destroys the infectious waste on the instruments, equipment, glassware, utensils, and materials.

The MEO process will operate in two modes (sterilization and disinfection). In the first mode (sterilization) the MEO process will precede until complete destruction of all the infectious waste on the instruments, equipment, glassware, utensils, and materials is accomplished. The second mode (disinfection) the MEO process is modified to stop the process at a point where the destruction of the infectious waste is incomplete but the infectious materials are benign and do not need further treatment.

Referring to FIG. 1A, the infectious waste on the instruments, equipment, glassware, utensils, and materials may be a liquid, solid, or a mixture of solids and liquids. Hinged lid 1 is lifted, the instruments, equipment, glassware, utensils, and/or materials are introduced into the of EG Basket 3 in the reaction chamber 5 a where they remains while the liquid portion of the infectious waste will flow into the anolyte. The EG Basket 3 sits on a rack 36 which is raised and lowered when the lid 1 is raised. When the Lid 1 is opened the anolyte fluid is lowered to a level below the rack 36 so as to avoid contact with the anolyte fluid. The apparatus continuously circulates the anolyte portion of the electrolyte directly from the electrochemical cell 25 through the reaction chamber 5 a to maximize the concentration of oxidizing species contacting the infectious waste. An in-line filter 6 prevents solid particles large enough to clog the electrochemical cell 25 flow paths from exiting the reaction chamber 5 a. Contact of the oxidizing species with incomplete oxidation products that are gaseous at the conditions within the reaction chamber 5 a may be enhanced by using conventional techniques for promoting gas/liquid contact (e.g., ultrasonic vibration 9, mechanical mixing 7). All surfaces of the apparatus in contact with the anolyte or catholyte are composed of stainless steel, glass, or nonreactive polymers (e.g., PTFE, PTFE lined tubing, etc.

The anolyte circulation system contains a pump 19 and a removal and treatment system 15 (e.g., filter, centrifuge, hydrocyclone, etc,) to remove any insoluble inorganic compounds that form as a result of mediator or electrolyte ions reacting with anions of or containing halogens, sulfur, phosphorous, nitrogen, etc. that may be present in the infectious waste stream thus preventing formation of unstable oxycompounds (e.g., perchlorates, etc.). The anolyte is then returned to the electrochemical cell 25, where the oxidizing species are regenerated, which completes the circulation in the anolyte system (A).

The instruments, equipment, glassware, utensils, and/or materials may be added to the EG Basket 3 in the reaction chamber either continuously or in the batch mode. The anolyte starts either at the operating temperature or at a lower temperature, which subsequently is increased by the thermal control 21 to the desired operating temperature for the specific infectious waste stream. The instruments, equipment, glassware, utensils, and/or materials may also be introduced into the apparatus, with the concentration of electrochemically generated oxidizing species in the anolyte being limited to some predetermined value between zero and the maximum desired operating concentration for the infectious waste stream by control of the electric current by the system dc power supply 29 supplied to the electrochemical cell 25. The electrolyte is composed of an aqueous solution of mediator species and electrolytes appropriate for the species selected and is operated within the temperature range from approximately 0° C. to slightly below the boiling point of the electrolytic solution, usually less then 100° C., at a temperature or temperature profile most conducive to the desired infectious waste destruction rate (e.g., most rapid, most economical, etc.). The acid, alkaline, or neutral salt electrolyte used will be determined by the conditions in which the species will exist.

Considerable attention has been paid to halogens especially chlorine and their deleterious interactions with silver mediator ions, however this is of much less concern or importance to this invention for the following two reasons. First, the infectious waste considered herein typically contains relatively small amounts of these halogen elements compared to the halogenated solvents and nerve agents addressed in the cited patents. Second, the wide range of properties (e.g., oxidation potential, solubility of compounds, cost, etc.) of the mediator species claimed in this patent allows selection of a single or mixture of mediators either avoiding formation of insoluble compounds, easily recovering the mediator from the precipitated materials, or being sufficiently inexpensive so as to allow the simple disposal of the insoluble compounds as waste, while still maintaining the capability to oxidize (i.e., destroy) the infectious waste economically.

The residue of the inorganic compounds is flushed out of the treatment system 15 during periodic maintenance if necessary. If warranted, the insoluble inorganic compounds are converted to water-soluble compounds using any one of several chemical or electrochemical processes.

The sterilization and disinfection processes will be monitored by several electrochemical and physical methods. Various cell voltages (e.g., open circuit, anode vs. reference electrode, ion specific electrode, etc.) yield information about the ratio of oxidized to reduced mediator ion concentrations which will be correlated with the amount of reducing agent (i.e., infectious waste) either dissolved in or wetted by the anolyte. If a color change accompanies the transition of the mediator species between it's oxidized and reduced states (e.g., heteropoly blues, etc.), the rate of decay of the color associated with the oxidized state, under zero current conditions, could be used as a gross indication of the amount of reducing agent (i.e., oxidizable infectious waste) present. If no color change occurs in the mediator, it may be possible to select another mediator to simply serve as the oxidization potential equivalent of a pH indicator. Such an indicator will be required to have an oxidation potential between that of the working mediator and the infectious species, and a color change associated with the oxidization state transition.

The anode reaction chamber off-gas will consist of CO₂ and CO from complete and incomplete combustion (i.e., oxidation) of the carbonaceous material in the infectious waste, and possibly oxygen from oxidation of water molecules at the anode. Standard anesthesiology practice requires these three gases to be routinely monitored in real time under operating room conditions, while many other respiratory related medical practices also require real time monitoring of these gases. Thus a mature industry exist for the production of miniaturized gas monitors directly applicable to the continuous quantitative monitoring of anolyte off-gas for the presence of combustion products. Although usually not as accurate and requiring larger samples, monitors for these same gasses are used in the furnace and boiler service industry for flue gas analysis.

The entireties of U.S. Pat. Nos. 3,725,226, 4,202,740, 4,384,943, 4,686,019; 4,749,519; 4,874,485; 4,925,643; 5,364,508; 5,516,972; 5,745,835; 5,756,874; 5,810,995; 5,855,763; 5,911,868; 5,919,350; 5,952,542; and 6,096,283 are included herein by reference for their relevant teachings.

MEO Apparatus

The MEO process will operate in two modes (sterilization and disinfection). A schematic drawing of the MEO apparatus shown in FIG. 1A MEO Apparatus Diagram illustrates the application of the MEO process to the instruments, equipment, glassware, utensils, and/or materials to sterilize or disinfect them. The MEO apparatus is composed of two separate closed-loop systems containing an electrolyte solution composed of anolyte and catholyte solutions. The anolyte and catholyte solutions are contained in the anolyte (A) system and the catholyte (B) system, respectively. These two systems are discussed in detail in the following paragraphs. There are numerous variations on the configuration of the anolyte reaction chamber(s) 5(a,b,c,d) and the modes of operation. The anolyte reaction chamber has numerous configurations as represented by FIGS. 1B thru 1E. The configuration in FIG. 1B being used in mode one will be discussed as illustrative of the many anolyte reaction chambers and operation modes combinations. This combination will be discussed in detail in the following paragraphs.

ANOLYTE SYSTEM (A)

The bulk of the anolyte resides in the anolyte reaction chamber 5 a (FIG. 1B). The hinged lid 1 is raised and the contaminated instruments, equipment, glassware, utensils, and/or materials are placed in EG Basket 3 in the reaction chamber 5 a containing liquid, solid, or a mixture of liquids and solids infectious waste. The EG Basket 3 sits on a rack 36 which is raised and lowered when the lid 1 is raised. When the Lid 1 is opened the anolyte fluid is lowered to a level below the rack 36 so as to avoid contact with the anolyte fluid.

The anolyte portion of the electrolyte solution contains for example Fe⁺³/FeO₄ ⁻² redox couple anions and secondary oxidizing species (e.g., free radicals, •H₂O₂, etc.). The bulk of the anolyte resides in the anolyte reaction chamber 5 a. The anolyte is circulated into the reaction chamber 5 a through the electrochemical cell 25 by pump 19 on the anode 26 side of the membrane 27. A membrane 27 in the electrochemical cell 25 separates the anolyte portion and catholyte portion of the electrolyte. A filter 6 is located at the base of the reaction chamber 5 a to limit the size of the solid particles to approximately 1 mm in diameter (i.e., smaller than the minimum dimension of the anolyte flow path in the electrochemical cell 25). Small thermal control units 21 and 22 are connected to the flow stream to heat or cool the anolyte to the selected temperature range. The heat exchanger 23 lowers the temperature of the anolyte entering the electrochemical cell and the heat exchanger 24 raises the temperature before it enters the anolyte reaction chamber 5 a. The electrochemical cell 25 is energized by a DC power supply 29, which is powered by the AC power supply 30. The DC power supply 29 is low voltage high current supply usually operating below 10V DC but not limited to that range. The AC power supply 30 operates off a typical 110v AC line for the smaller units and 240v AC for the larger units.

The oxidizer species population produced by electrochemical generation (i.e., anodic oxidation) of the oxidized form of the redox couples referenced herein can be enhanced by conducting the process at low temperatures, thereby reducing the rate at which thermally activated parasitic reactions consume the oxidizer. If warranted a heat exchanger 23 can be located immediately upstream from the electrochemical cell 25 to lower the anolyte temperature within the cell to the desired level. Another heat exchanger 24 can be located immediately upstream of the anolyte reaction chamber inlet to control the anolyte temperature in the reaction chamber to within the desired temperature range to affect the desired chemical reactions at the desired rates.

The electrolyte containment boundary is composed of materials resistant to the oxidizing electrolyte (e.g., stainless steels, PTFE, PTFE lined tubing, glass, etc.). Reaction products resulting from the oxidizing processes occurring in the anolyte system (A) of the system that are gaseous at the anolyte operating temperature and pressure are discharged to the condenser 13. The more easily condensed products of incomplete oxidation are separated in the condenser 13 from the anolyte off-gas stream and are returned to the anolyte reaction chamber 5 a for further oxidation. The non-condensable incomplete oxidation products (e.g., low molecular weight organics, carbon monoxide, etc.) are reduced to acceptable levels for atmospheric release by a gas cleaning system 16. The gas cleaning system 16 is not a necessary component of the MEO apparatus for the destruction of most types of infectious waste on the instruments, equipment, glassware, utensils, and/or materials.

If the gas cleaning system 16 is incorporated into the MEO apparatus, the anolyte off-gas is contacted in a counter current flow gas scrubbing system in the off-gas cleaning system 16 wherein the noncondensibles from the condenser 13 are introduced into the lower portion of the column through a flow distribution system of the gas cleaning system 16 and a small side stream of freshly oxidized anolyte direct from the electrochemical cell 25 is introduced into the upper portion of the column. This will result in the gas phase continuously reacting with the oxidizing mediator species as it rises up the column past the down flowing anolyte. Under these conditions the gas about to exit the top of the column will have the lowest concentration of oxidizable species and will also be in contact with the anolyte having the highest concentration of oxidizer species thereby promoting reduction of any air pollutants present down to levels acceptable for release to the atmosphere. Gas-liquid contact within the column will be promoted by a number of well established methods (e.g., packed column, pulsed flow, ultrasonic mixing, etc,) that will not result in any meaningful back pressure within the anolyte flow system. Unique infectious waste compositions may result in the generation of unusual gaseous products that could more easily be removed by more traditional air pollution technologies. Such methodologies could be used in series with the afore described system as a polishing process treating the gaseous discharge from the counter current column, or if advantageous, instead of it. The major products of the oxidation process are CO₂, and water (including minor amounts of CO and inorganic salts), where the CO₂ is vented 14 out of the system.

An optional inorganic compound removal and treatment systems 15 is used should there be more than trace amount of halogens, or other precipitate forming anions present in the infectious waste being processed, thereby precluding formation of unstable oxycompounds (e.g., perchlorates, etc.).

The MEO process will proceed until complete destruction of the infectious waste has been affected on the instruments, equipment, glassware, utensils, and/or materials (sterilization) or be modified to stop the process at a point where the destruction of the infectious waste is incomplete (disinfection). The reason for stopping the process is that the infectious materials are benign and do not need further treatment. The organic compounds recovery system 17 is used to perform this process.

CATHOLYT SYSTEM (B)

The bulk of the catholyte is resident in the catholyte reaction chamber 31. The catholyte portion of the electrolyte is circulated by pump 43 through the electrochemical cell 25 on the cathode 28 side of the membrane 27. The membrane does not allow the infectious agents to cross from the anolyte into the catholyte. The catholyte portion of the electrolyte flows into a catholyte reservoir 31. Small thermal control units 45 and 46 are connected to the catholyte flow stream to heat or cool the catholyte to the selected temperature range. External air is introduced through an air sparge 37 into the catholyte reservoir 31. The oxygen contained in the air oxidizes nitrous acid and the small amounts of nitrogen oxides (NO_(x)), produced by the cathode reactions, to nitric acid and NO₂, respectively. Contact of the oxidizing gas with nitrous acid may be enhanced by using conventional techniques for promoting gas/liquid contact by a mixer 35 (e.g., ultrasonic vibration 48, mechanical mixing 35, etc.). Systems using non-nitric acid catholytes may also require air sparging to dilute and remove off-gas such as hydrogen. An off-gas cleaning system 39 is used to remove any unwanted gas products (e.g. NO₂, etc.). The cleaned gas stream, combined with the unreacted components of the air introduced into the system is discharged through the atmospheric vent 47.

Optional anolyte recovery system 41 is positioned on the catholyte side. Some mediator oxidizer ions may cross the membrane 27 and this option is available if it is necessary to remove them through the anolyte recovery system 41 to maintain process efficiency or cell operability, or their economic worth necessitates their recovery. Operating the electrochemical cell 25 at higher than normal membrane 27 current densities (i.e., above about 0.5 amps/cm²) will increase the rate of infectious waste destruction, but also result in increased mediator ion transport through the membrane into the catholyte. It may be economically advantageous for the electrochemical cell 25 to be operated in this mode. It is advantageous whenever the replacement cost of the mediator species or removal/recovery costs are less than the cost benefits of increasing the infectious waste throughput (i.e., oxidation rate) of the electrochemical cell 25. Increasing the capitol cost of expanding the size of the electrochemical cell 25 can be avoided by using this operational option.

SYSTEM MODEL

A preferred embodiment, MEO System Model 5.b (shown in FIG. 2 MEO System Model 5.b) is sized for use on the ward of a hospital or in a small medical or veterinary laboratory. Other preferred embodiments have differences in the external configuration and size but are essentially the same in internal function and components as depicted in FIGS. 1A through FIG. 1E. The preferred embodiment in FIG. 2 comprises a housing 72 constructed of metal or high strength plastic surrounding the electrochemical cell 25, the electrolyte and the foraminous EG Basket 3. The AC power is provided to the AC power supply 30 by the power cord 78. A monitor screen 51 is incorporated into the housing 72 for displaying information about the system and about the infectious waste being treated. Additionally, a control keyboard 53 is incorporated into the housing 72 for inputting information into the system. The monitor screen 51 and the control keyboard 53 may be attached to the system without incorporating them into the housing 72. In a preferred embodiment, status lights 73 are incorporated into the housing 72 for displaying information about the status of the treatment of the infectious waste on the instruments, equipment, glassware, utensils, and/or materials. An air sparge 37 is incorporated into the housing 72 to allow air to be introduced into the catholyte reaction chamber 31 below the surface of the catholyte. In addition, a CO₂ vent 14 is incorporated into the housing 72 to allow for CO₂ release from the anolyte reaction chamber housed within. In a preferred embodiment, the housing includes means for cleaning out the MEO infectious waste treatment system, including a flush(s) 18 and drain(s) 12 through which the anolyte and catholyte will pass. The preferred embodiment further comprises an atmospheric vent 47 facilitating the releases of gases into the atmosphere from the catholyte reaction chamber 31. Other preferred embodiment systems are similar in nature but are scaled up in size to handle a larger capacity of instruments, equipment, glassware, utensils, and/or materials containing infectious waste, such as operating rooms, laboratories, incinerator replacement units, etc.

The system has a control keyboard 53 for input of commands and data. The On/Off button 74 is used to turn the apparatus power on and off. There is a monitor screen 51 to display the systems operation and functions. Below the keyboard 53 and monitor screen 51 are the status lights 73 for on, off, and standby. Hinged lid 1 is opened and the contaminated instruments, equipment, glassware, utensils, and/or materials are deposited in the EG Basket 3 in the chamber 5 a. A lid stop 2 keeps the lid opening controlled. The hinged lid 1 is equipped with a locking latch 76 that is operated by the controller 49. In the chamber 5 a is the aqueous acid, alkali, or neutral salt electrolyte and mediated oxidizer species solution in which the oxidizer form of the mediator redox couple initially may be present or may be generated electrochemically after introduction of the infectious waste and application of DC power 30 to the electrochemical cell 25. Similarly, the contaminated instruments, equipment, glassware, utensils, and/or materials will be introduced when the anolyte is at room temperature, operating temperature or some optimum intermediate temperature. DC power supply 30 provides direct current to an electrochemical cell 25. Pump 19 circulates the anolyte portion of the electrolyte and the infectious waste material is rapidly oxidized at temperatures below 100° C. and ambient pressure. An in-line filter 6 prevents solid particles large enough to clog the electrochemical cell 25 flow paths from exiting this reaction chamber 5 a. The oxidation process will continue to break the materials down into smaller and smaller molecules until they reach CO₂, water, and some CO and inorganic salts. Any residue is pacified in the form of a salt and may be periodically removed through the Inorganic Compound Removal and Treatment System 15 and drain outlets 12. The electrolyte can be replaced with a different electrolyte when using the same plumbing for their introduction into the reaction chambers 5 and 31 changes the application or contaminating infectious waste to be destroyed. The catholyte reservoir 31 has a screwed top 33 (shown in FIG. 1A), which allow access to the reservoir 31 for cleaning and maintenance by service personnel.

The MEO apparatus as an option may be placed in a standby mode with the contaminated instruments, equipment, glassware, utensils, and/or materials being added as they are generated throughout the day and the unit placed in full activation during non-business hours. The MEO process advantageous properties of low power consumption and very low loses of the mediated oxidizer species and electrolyte, provide as an option for the device to be operated at a low level during the day to achieve a slow rate of destruction of the infectious waste throughout the day.

The compactness and scalability of the device makes it ideal for medical/dental/veterinary offices and operating rooms as well as being suitable for use with high volume inputs of laboratories and hospitals non-operating room activities. The process operates at low temperature and ambient atmospheric pressure and does not generate toxic compounds during the destruction of the infectious waste, making the process indoors compatible. The system is scalable to a unit large enough to replace a hospital incinerator system. The CO₂ oxidation product from the anolyte system A is vented out the CO₂ vent 14. The off-gas products from the catholyte system B is vented through the atmospheric air vent 47 as shown.

SYSTEM CONTROLLER

An operator runs the MEO Apparatus (FIG. 1A, FIG. 1B, FIG. 2) by using the MEO Controller depicted in FIG. 3 MEO Controller. The controller 49 with microprocessor is connected to a monitor 51 and a keyboard 53. The operator inputs commands to the controller 49 through the keyboard 53 responding to the information displayed on the monitor 51. The controller 49 runs a program that sequences the steps for the operation of the MEO apparatus. The program has pre-programmed sequences of standard operations that the operator will follow or he will choose his own sequences of operations. The controller 49 will allow the operator to select his own sequences within limits that assure a safe and reliable operation. The controller 49 sends digital commands that regulates the electrical power (AC 30 and DC 29) to the various components in the MEO apparatus; pumps 19 and 43, mixers 7 and 35, thermal controls 21, 22, 45, 46, ultraviolet sources 11, ultrasonic sources 9 and 48, CO₂ vent 14, air sparge 37, and electrochemical cell 25. The controller receives component response and status from the components. The controller sends digital commands to the sensors to access sensor information through sensor responses. The sensors in the MEO apparatus provide digital information on the state of the various components. Sensors measure flow rate 59, temperature 61, pH 63, CO₂ venting 65, degree of oxidation 67, air sparge sensor 69, etc. The controller 49 receives status information on the electrical potential (voltmeter 57) across the electrochemical cell, or individual cells if a multi-cell configuration, and between the anode(s) and reference electrodes internal to the cell(s) 25 and the current (ammeter 55) flowing between the electrodes within each cell.

STEPS OF THE OPERATION OF THE MEO PROCESS

The steps of the operation of the MEO process are depicted in FIG. 4 MEO System Operational Steps. This MEO apparatus is contained in the housing 72. The MEO system is started 81 by the operator engaging the ‘ON’ button 74 (status lights 73) on the control keyboard 53. The system controller 49, which contains a microprocessor, runs the program that controls the entire sequence of operations 82. The monitor screen 51 displays the steps of the process in the proper sequence. The status lights 73 on the panel provide the status of the MEO apparatus (e.g. on, off, ready, standby). The lid 1 is opened and the contaminated instruments, equipment, glassware, utensils, and/or materials (which can be in liquid, solid, and a mixture)are placed 83 in the EG Basket 3, whereupon the instruments, equipment, glassware, utensils, and/or materials are retained and the liquid portion flows through the EG Basket 3 and into the anolyte. The locking latch 76 is activated. The pumps 19 and 43 begin circulation 85 of the anolyte 87 and catholyte 89, respectively. As soon as the electrolyte circulation is established throughout the system, the mixers 7 and 35 begin to operate 91 and 93. Depending upon infectious waste characteristics (e.g., reaction kinetics, heat of reaction, etc.) it may be desirable to introduce the contaminated instruments, equipment, glassware, utensils, and/or materials into a room temperature or cooler anolyte system with little or none of the mediator redox couple in the oxidizer form. Once flow is established the thermal controls units 21, 22, 45, and 46 are turned on 95/97, initiating predetermined anodic oxidation and electrolyte heating programs. The electrochemical cell 25 is energized 94 (by cell commands 56) to the electric potential 57 and current 55 density determined by the controller program. By using programmed electrical power and electrolyte temperature ramps it is possible to maintain a predetermined infectious waste destruction rate profile such as a relatively constant reaction rate as the more reactive infectious waste components are oxidized, thus resulting in the remaining infectious waste becoming less and less reactive, thereby requiring more and more vigorous oxidizing conditions. The ultrasonic 9 and 48 and ultraviolet systems 11 are activated 99 and 101 in the anolyte reaction chamber 5 a and catholyte reaction chamber 31 if those options are chosen in the controller program. The CO₂ vent 14 is activated 103 to release CO₂ from the infectious waste oxidation process in the anolyte reaction chamber 5 a. The air sparge 37 and atmospheric vent 47 are activated 105 in the catholyte system. The progress of the destruction process will be monitored in the controller (oxidation sensor 67) by various cell voltages and currents 55, 57 (e.g., open circuit, anode vs. reference electrode, ion specific electrodes, etc,) as well as monitoring anolyte off-gas (using the sensor 65) composition for CO₂, CO and oxygen content.

The infectious waste is being decomposed into water and CO₂ the latter being discharged 103 out of the CO₂ vent 14. Air sparge 37 draws air 105 into the catholyte reservoir 31, and excess air is discharged out the atmospheric vent 47. When the oxidation sensors 65 and 67 determine the desired degree of infectious waste destruction has been obtained 107, the system goes to standby 109. The system operator executes system shutdown 111 using the controller keyboard 53.

EXAMPLES

The following examples illustrate the application of the process and the apparatus.

Example (1)

Destruction of Biological Specimens:

The MEO apparatus using the MEO process was tested using a number of whole small animals (dead mice). The MEO process was run at less then 100 watts for approximately an hour. The entire physical structure of the mouse was totally converted into a liquid. The liquid was tested using GC/FID analysis and did not show evidence of any hydrocarbons present. The detection limit for this analysis method (GC/FID) is approximately 1 to 10 ppm (parts per million). This result supports the conclusion that the contents of the liquid were sterile and disinfected. The microorganism tests to determine the existence of microorganism will be completed following accepted protocols to substantiate the conclusion that the MEO process destroys the infectious waste on the instruments, equipment, glassware, utensils, and materials.

Example (2)

Efficient and Environmentally Safe Products:

The MEO process produces CO₂, water, and trace inorganic salts all of which are considered benign for introduction into the environment by regulatory agencies. The cost of using the MEO process in this invention is competitive with both the incineration and landfill methodologies. The MEO process is uniquely suited for destruction of infectious waste because water, which constitutes a major portion of this infectious waste (e.g., tissue, bodies fluids, etc.) is either benign or actually a source of secondary oxidizing species, rather than parasitic reactions competing for the mediator oxidizing species. Furthermore, the energy that must be provided in the MEO process to heat the infectious waste stream water component from ambient to the electrolyte operating temperature (i.e., 80° C. maximum temperature increase) is trivial compared to the water enthalpy increase required in autoclave or incineration based processes.

Example (3)

Benign In-door Operation:

The system is unique relative to earlier art, since it is built to operate in an indoor environment such as a hospital room or laboratory where it must be compatible with people working in close proximity to the system as well as people being treated for medical conditions. The system is suitable for indoor use in spaces inhabited by personnel as well as for industrial workspaces similar to an incinerator building.

Example (4)

Inheritantly Safe Operation:

The system is built to require limited operating skill. The system controller is programmed to guide the operator through the normal operating cycle as well as the various options available. The system is accessible during its operating cycle so that additional contaminated instruments, equipment, glassware, utensils, and/or materials may be added to infectious waste in process, while remaining compatible with the room environment. The physical sterilization methods such as autoclaves are not as flexible and can not be stopped during their operating cycle. When new contaminated instruments, equipment, glassware, utensils, and/or materials are to be added to the system during operation the operator selects that option. The system controller recycles the system operational steps back to step 83. It deactivates steps 85, 87, 89, 91, 93, 94, 95, 97, 99, 101 and maintains steps 103 and 105 in their active mode. The controller releases the locking latch 76 and the operator will add additional contaminated instruments, equipment, glassware, utensils, and/or materials. After he has completed the addition he selects the restart option. The system recycles back through these steps to continue the processing of the infectious waste.

Example (5)

Chemical Reactions are Safe:

The system is built to operate with materials that are safe to handle in the environment in which it is to be used. The infectious waste contains little or no substances that react with our choice of electrolytes to produce volatile compounds that will offer a problem in the room environment. The system will operate at temperatures from approximately 0° C. to slightly less then the boiling point of the electrolyte, which is usually less then 100° C. and at ambient atmospheric pressure, which adds to the indoor compatibility.

Example (6)

A Green Machine:

The simplicity of the new system built for use with contaminated instruments, equipment, glassware, utensils, and/or materials produces a system more economically to operate and cleaner to use than existing infectious waste treatments. In the case of commonly used disinfection methods such as chlorine compounds, iodines, alcohols, ammonium, and aldehydes. The system complexity is reduced by comparison to previous MEO systems, since there is not a requirement to deal with large quantities of halogens. The system is truly a ‘green machine’ in the sense of an environmentally benign system.

Example (7)

System Flexibility:

The system is built so that the composition of the electrolyte may be changed to adapt the system to a selected composition of the infectious waste stream. The system is configured with ports to flush and drain the anolyte and catholyte separately.

Example (8)

System By-Products are Safe:

The system flexibility provides for the introduction of more then one mediator ion resulting in marked improvement in the efficiency of the electrolyte. Furthermore, it desensitizes the electrolyte to chlorine ions in solution (i.e. allows increased ease in preventing formation of unstable perchlorate compounds).

While the invention has been described with reference to specific embodiments, modifications and variations of the invention may be constructed without departing from the scope of the invention, which is defined in the following characteristics and features.

The invention provides the following new characteristics and features:

-   1. A process for sterilizing/disinfecting by treating and oxidizing     infectious waste materials on the contaminated instruments,     equipment, glassware, utensils, and/or materials comprising     disposing an electrolyte in an electrochemical cell, separating the     electrolyte into an anolyte portion and a catholyte portion with an     ion-selective membrane or semipermeable membrane applying a direct     current voltage between the anolyte portion and the catholyte     portion, placing the contaminated instruments, equipment, glassware,     utensils, and/or materials in the anolyte portion, and oxidizing the     infectious waste materials in the anolyte portion with a mediated     electrochemical oxidation (MEO) process, wherein the anolyte portion     further comprises a mediator in aqueous solution and the electrolyte     is an acid, neutral or alkaline aqueous solution. -   2. The process of paragraph 1, wherein:     -   a. the anolyte portion further comprises one or more simple         anions mediator ion: species selected from the group described         in Table I (in the aqueous solution and the electrolyte is an         acid, neutral or alkaline solution;     -   b. The oxidizing species are selected from one or more Type I         isopolyanions (i.e., complex anion redox couple mediators)         containing tungsten, molybdenum, vanadium, niobium, tantalum, or         combinations thereof as addenda atoms in aqueous solution and         the electrolyte is an acid, neutral or alkaline aqueous         solution;     -   c. The oxidizing species are selected from one or more Type I         heteropolyanions formed by incorporation into the aforementioned         isopolyanions, as heteroatoms, any of the elements listed in         Table II, either singly or in combination thereof in the aqueous         solutions and the electrolyte is an acid, neutral, or alkaline         aqueous solution;     -   d. The oxidizing species are selected from one or more of any         heteropolyanions containing at least one heteroatom type (i.e.,         element) contained in both Table I and Table II_in the aqueous         solutions_and the_electrolyte is an acid, neutral, or alkaline         aqueous solution;     -   e. The oxidizing species are selected from combinations of anion         redox couple mediators from any or all of the previous four         subparagraphs (2 a., 2 b., 2 c., and 2 d.);     -   f. adding stabilizing compounds to the electrolyte such as         tellurate or periodate ions which serve to overcome and         stabilize the short lifetime of the oxidized form of the higher         oxidation state species of the simple and complex anion redox         couple mediators;     -   g. the oxidizing species are elements having atomic numbers less         than 90 and identified in Table I;     -   h. each of the species has normal valence states and higher         valence oxidizing states and further comprising creating the         higher valence oxidizing states of the oxidizing species by         stripping electrons from normal valence state species in the         electrochemical cell;     -   i. the oxidizing species are “super oxidizers” (SO) typically         exhibit oxidation potentials at least equal to that of the         Ce⁺³/Ce⁺⁴ redox couple (i.e., 1.7 volts at 1 molar, 25° C. and         pH 1) which are redox couple species that have the capability of         producing free radicals such as hydroxyl or perhydroxyl and         further comprising creating secondary oxidizers by reacting the         SO's with water;     -   j. using an alkaline solution for aiding decomposing of the         infectious waste materials derived from the saponification         (i.e., base promoted ester hydrolysis) of fatty acids to form         water soluble alkali metal salts of the fatty acids (i.e.,         soaps) and glycerin, a process similar to the production of soap         from animal fat by introducing it into a hot aqueous lye         solution.;     -   k. using an alkaline anolyte solution that absorbs CO₂ forming         from oxidation of the infectious waste sodium         bicarbonate/carbonate solution which subsequently circulates         through the electrochemical cell, producing a percarbonate         oxidizer;     -   l. using oxidizing species from the MEO process inorganic free         radicals will be generated in aqueous solutions from species         such as but not limited to carbonate, azide, nitrite, nitrate,         phosphite, phosphate, sulfite, sulfate, selenite, thiocyanate,         chloride, bromide, iodide, and formate oxidizing species;     -   m. the regeneration of the oxidizer part of the redox couple in         the anolyte portion is done within the electrochemical cell;     -   n. the membrane(separator between anolyte and catholyte         solutions) can be microporous plastic, sintered glass frit,         etc.;     -   o. the impression of an AC voltage upon the DC voltage to retard         the formation of cell performance limiting surface films on the         electrode;     -   p. disposing a foraminous EG Basket 3 in the anolyte;     -   q. adding oxygen (this is necessary only for HNO₃ ⁻ or NO₃ ⁻         salts) to the catholyte portion;     -   r. the oxidizer species addressed in this patent are described         in: Table I (simple anions); Type I isopolyanions containing         tungsten, molybdenum, vanadium, niobium, tantalum, or         combinations thereof as addenda atoms; Type I heteropolyanions         formed by incorporation into the aforementioned isoopolyanions,         as heteroatoms, any of the elements listed in Table II, either         singly or in combinations thereof; or any heteropolyanions         containing at least one heteroatom type (i.e., element)         contained in both Table I and Table II;     -   s. lower the temperature (e.g. between 0° C. and room         temperature) of the anolyte before it enters the electrochemical         cell to enhance the generation of the oxidized form of the anion         redox couple mediator; and     -   t. raise the temperature of the anolyte entering the anolyte         reaction chamber to affect the desired chemical reactions at the         desired rates following the lowering of the temperature of the         anolyte entering the electrochemical cell. -   3. The process of paragraph 1, wherein:     -   a. introducing an ultrasonic energy into the anolyte portion         rupturing cell membranes in the infectious waste materials by         momentarily raising local temperature within the cell membranes         with the ultrasonic energy to above several thousand degrees and         causing cell membrane failure;     -   b. introducing ultraviolet energy into the anolyte portion and         decomposing hydrogen peroxide and ozone into hydroxyl free         radicals therein, thereby increasing efficiency of the MEO         process by converting products of electron consuming parasitic         reactions (i.e., ozone and hydrogen peroxide) into viable free         radical (i.e., secondary) oxidizers without the consumption of         additional electrons;     -   c. using a surfactant to be added to the anolyte promote         dispersion of the infectious waste or intermediate stage         reaction products within the aqueous solution when these         infectious waste or reaction products are not water-soluble and         tend to form immisible layers;     -   d. using simple and/or complex redox couple mediators, and         attacking specific organic molecules with the oxidizing species         while operating at low temperatures thus preventing the         formation of dioxins and furans;     -   e. breaking down infectious waste materials into organic         compounds and attacking the organic compounds using either the         simple and/or complex anion redox couple mediator or inorganic         free radicals to generating organic free radicals;     -   f. raising normal valence state anions to a higher valence state         and stripping the normal valence state anions of electrons in         the electrochemical cell; [The oxidized forms of any other redox         couples present are produced either by similar anodic oxidation         or reaction with the oxidized form of other redox couples         present. The oxidized species of the redox couples oxidize the         infectious waste molecules and are themselves converted to their         reduced form, whereupon they are reoxidized by either of the         aforementioned mechanisms and the redox cycle continues]     -   g. circulating anions through an electrochemical cell to affect         the anodic oxidation of the reduced form of the reversible redox         couple into the oxidized form;     -   h. contacting anions with infectious waste materials in the         anolyte portion;     -   i. circulating anions through the electrochemical cell;     -   j. involving anions with an oxidation potential above a         threshold value of 1.7 volts (i.e., superoxidizer) in a         secondary oxidation process and producing oxidizers;     -   k. adding a ultra-violet (UV) energy source to the anolyte         portion and augmenting secondary oxidation processes, breaking         down hydrogen peroxide and ozone into hydroxyl free radicals,         and thus increasing the oxidation processes;     -   l. introducing an ultrasonic energy source into the anolyte         portion and irradiating cell membranes in infectious waste         materials and momentarily raising local temperature within the         cell membranes and causing cell membrane failure creating         greater exposure of cell contents to oxidizing species in the         anolyte portion; and     -   m. The oxidizer species addressed in this patent (I.e.,         characteristic elements having atomic number below 90) are         described in Table I (simple anions redox couple mediators):         Type I IPAs formed by Mo, W, V, Nb, Ta, or mixtures there of;         Type I HPAs formed by incorporation into the aforementioned IPAs         if any of the elements listed in Table II (heteroatoms) either         singly or in thereof; Or any HPA containing at least one         heteroatom type (i.e., element) contained in both Table I and         Table II or combinations mediator species from any or all of         these generic groups. -   4. The process of paragraph 1, further comprising:     -   a. using oxidizer species that are found in situ in the,         infectious waste to be destroyed, by circulating the infectious         waste-anolyte mixture through an electrochemical cell where the         oxidized form of the in situ reversible redox couple will be         formed by anodic oxidation or alternately reacting with the         oxidized form of a more powerful redox couple, if added to the         anolyte and anodically oxidized in the electrochemical cell,         thereby destroying the infectious waste material;     -   b. using an alkaline electrolyte, such as but not limited to         NaOH or KOH with mediator species wherein the reduced form of         said mediator redox couple displays sufficient solubility in         said electrolyte to allow the desired oxidation of the         infectious waste to proceed at a practical rate. The oxidation         potential of redox reactions producing hydrogen ions (i.e., both         mediator species and infectious waste molecules reactions) are         inversely proportional to the electrolyte pH, thus with the         proper selection of a mediator redox couple, it is possible, by         increasing the electrolyte pH, to minimize the electric         potential required to affect the desired oxidation process,         thereby reducing the electric power consumed per unit mass of         infectious waste destroyed; and     -   c. the aqueous solution is chosen from acids such as but not         limited to nitric acid, sulfuric acid, or phosphoric acid, or         mixtures thereof; or alkalines such as but not limited to of         sodium hydroxide or potassium hydroxide, or mixtures thereof, or         neutral electrolytes,. such as but not limited to sodium or         potassium nitrates, sulfates, or phosphates or mixtures thereof.     -   d. the use of ultrasonic energy induce microscopic bubble         implosion which will be used to affect a desired reduction in         sized of the individual second phase infectious waste volumes         dispersed in the anolyte. -   5. The process of paragraph 1, further comprising:     -   a. interchanging oxidizing species in a preferred embodiment         without changing equipment; and     -   b. the electrolyte is acid, neutral, or alkaline in aqueous         solution. -   6. The process of paragraph 1, further comprising:     -   a. separating the anolyte portion and the catholyte portion with         a ion-selective or semi-permeable membrane, or microporous         polymer membrane, ceramic membrane, or sintered glass frit, or         other similar membrane;     -   b. applying an externally induced electrical potential induced         between the anode(s) and cathode(s) plates of the         electrochemical cell at a electrical potential sufficient to         form the oxidized form of the redox couple having the highest         oxidation potential in the anolyte;     -   c. introducing contaminated instruments, equipment, glassware,         utensils, and materials into the anolyte portion;     -   d. forming the reduced form of one or more reversible redox         couples by contacting with oxidizable molecules, the reaction         with which oxidizes the oxidizable material with the concuminent         reduction of the oxidized form of the reversible redox couples         to their reduced form;     -   e. the ultrasonic source connected to the anolyte for augmenting         secondary oxidation processes by momentarily heating the         hydrogen peroxide in the electrolyte to 4800° C. at 1000         atmospheres thereby dissociating the hydrogen peroxide into         hydroxyl free radicals thus increasing the oxidation processes;     -   f. oxidation potentials of redox reactions producing hydrogen         ions are inversely related to pH;     -   g. the process is performed at a temperature from slightly above         0° C. to slightly below the boiling point of the electrolyte         usually less then 100° C.;     -   h. the temperature at which the process is performed is varied;     -   i. the sterilizing and disinfecting contaminated instruments,         equipment, glassware, utensils, and materials comprises treating         and oxidizing liquid infectious waste;     -   j. the sterilizing and disinfecting contaminated instruments,         equipment, glassware, utensils, and materials comprises treating         and oxidizing solid infectious waste;     -   k. the sterilizing and disinfecting contaminated instruments,         equipment, glassware, utensils, and materials comprises treating         and oxidizing a combination of solid and liquid infectious         waste; and     -   l. removing and treating precipitates resulting from         combinations of oxidizing species and other species released         from the infectious waste during destruction. -   7. The process of paragraph 1, further comprising that it is not     necessary for both the anolyte and catholyte solutions to contain     the same electrolyte rather each electrolyte system may be     independent of the other, consisting of an aqueous solution of     acids, typically but not limited to nitric, sulfuric or phosphoric;     alkali, typically but not limited to sodium or potassium hydroxide;     or neutral salt, typically but not limited to sodium or potassium     salts of the afore mentioned strong acids. -   8. The process of paragraph 1, further comprising the operating of     the electrochemical cell at a current density greater then 0.5 amp     per square centimeter across the membrane, even though this is the     limit over which there is the possibility that metallic anions may     leak through the membrane in small quantities, and recovering the     metallic anions through a devise such as a resin column thus     allowing a greater rate of destruction of materials in the anolyte     chamber. -   9.The process of paragraph 1, wherein:     -   a. the catholyte solution further comprises an aqueous solution         and the electrolyte in the solution is composed of acids,         typically but not limited to nitric, sulfuric or phosphoric; or         alkali, typically but not limited to sodium or potassium         hydroxide; or neutral salt, typically but not limited to sodium         or potassium salts of the afore mentioned strong acids;     -   b. adding oxygen (this is necessary only for HNO₃ ⁻ or NO₃ ⁻         salts) to the catholyte portion;     -   c. concentration of electrolyte in the catholyte will be         governed by its effect upon the conductivity of the catholyte         solution desired in the electrochemical cell;     -   d. ultrasonic energy induced microscopic bubble implosion will         be used to affect vigorous mixing in the catholyte solution         where it is desirable to oxidize nitric acid and the small         amounts of nitrogen oxides when nitric acid is used in the         catholyte electrolyte;     -   e. mechanical mixing will be used to affect vigorous mixing in         the catholyte solution where it is desirable to oxidize nitric         acid and the small amounts of nitrogen oxides;     -   f. air is introduced into the catholyte solution to promote         oxidation of nitric acid and the small amounts of nitrogen         oxides when nitric acid is used in the catholyte electrolyte;     -   g. air is introduced into the catholyte solution to dilute any         hydrogen produced in the catholyte solution before being         released; and     -   h. hydrogen gas evolving from the cathode is feed to an         apparatus that uses hydrogen as a fuel such as a proton exchange         membrane (PEM) fuel cell. -   10. An apparatus for sterilizing/disinfecting by treating and     oxidizing infectious waste materials comprising an electrochemical     cell, an electrolyte disposed in the electrochemical cell, a     hydrogen or hydronium ion-permeable membrane, disposed in the     electrochemical cell for separating the cell into anolyte and     catholyte chambers and separating the electrolyte into anolyte and     catholyte portions, electrodes further comprising an anode and a     cathode disposed in the electrochemical cell respectively in the     anolyte and catholyte chambers and in the anolyte and catholyte     portions of the electrolyte, a power supply connected to the anode     and the cathode for applying a direct current voltage between the     anolyte and the catholyte portions of the electrolyte, a foraminous     EG Basket disposed in the anolyte chamber for receiving the     infectious waste materials, and oxidizing of the infectious waste     materials in the anolyte portion with a mediated electrochemical     oxidation (MEO) process wherein the anolyte portion further     comprises a mediator in aqueous solution and the electrolyte is an     acid, neutral or alkaline aqueous solution. -   11. The apparatus of paragraph 10, wherein:     -   a. adding stabilizing compounds to the electrolyte such as         tellurate or periodate ions which serve to overcome and         stabilize the short lifetime of the oxidized form of the higher         oxidation state species of the simple and complex anion redox         couple mediators;     -   b. the oxidizer species addressed in this patent (i.e.,         characteristic elements having atomic number below 90) are         described in Table I (simple anions redox couple mediators);     -   c. the oxidizer species addressed in this patent are; Type I         IPAs formed by Mo, W, V, Nb, Ta, or mixtures there of; Type I         HPAs formed by incorporation into the aforementioned IPAs if any         of the elements listed in Table II (heteroatoms) either singly         or in thereof; Or any HPA containing at least one heteroatom         type (i.e., element) contained in both Table I and Table II;     -   d. the oxidizer species addressed in this patent are         combinations mediator species from any or all of these generic         groups;     -   e. the oxidizing species are super oxidizers and further         comprising creating secondary oxidizers by reacting the super         oxidizers with the aqueous anolyte;     -   f. an alkaline solution for aiding decomposing the infectious         waste materials;     -   g. an alkaline solution for absorbing CO₂ and forming alkali         metal bicarbonate/carbonate for circulating through the         electrochemical cell for producing a percarbonate oxidizer;     -   h. using oxidizing species from the MEO process inorganic free         radicals will be generated in aqueous solutions derived from         carbonate, azide, nitrite, nitrate, phosphite, phosphate,         sulfite, sulfate, selenite, thiocyanate, chloride, bromide,         iodide, and formate oxidizing species;     -   i. organic free radicals for aiding the MEO process and breaking         down the infectious waste materials into simpler (i.e., smaller         molecular structure )organic compounds;     -   j. anions with an oxidation potential above a threshold value of         1.7 volts (i.e., super oxidizer) for involving in a secondary         oxidation process for producing oxidizers;     -   k. the use of Ultrasonic energy induce microscopic bubble         implosion which is used to affect a desired reduction in sized         of the individual second phase infectious waste volumes         dispersed in the anolyte;     -   l. membrane is ion-selective or semi-permeable (i.e.,         microporous plastic, ceramic, sintered glass frit, etc.).;     -   m. with the possible impression of an AC voltage upon the DC         voltage to retard the formation of cell performance limiting         surface films on the electrode; and     -   n. external air is introduced through an air sparge into the         catholyte reservoir where oxygen contained in the air oxidizes         nitrogen compounds produced by the cathode reactions (this is         necessary only when nitrogen compounds can occur in the         catholyte). -   12. The apparatus of paragraph 10, wherein:     -   a. each of the oxidizing species has normal valence states         (i.e., reduced form of redox couple) and higher valence         oxidizing states and further comprising creating the higher         valence oxidizing states (i.e., oxidized form of redox couple)of         the oxidizing species by stripping and reducing electrons off         normal valence state species in the electrochemical cell;     -   b. using species that are usable in alkaline solutions since         oxidation potentials of redox reactions producing hydrogen ions         are inversely related to pH which reduces the electrical power         required to destroy the infectious waste;     -   c. further oxidizing species, and attacking specific organic         molecules with the oxidizing species while operating at         temperatures sufficiently low so as to preventing the formation         of dioxins and furans;     -   d. a perbromate for treating medical sharps as identified under         the definition of infectious waste hereto referred;     -   e. energizing the electrochemical cell at a potential level         sufficient to form the oxidized form of the redox couple having         the highest oxidation potential in the anolyte;     -   f. lower the temperature (e.g. between 0° C. and room         temperature) of the anolyte with the heat exchanger before it         enters the electrochemical cell to enhance the generation of the         oxidized form of the anion redox couple mediator; and     -   g. raise the temperature of the anolyte (to the range ˜20 °C. to         80° C.) entering the anolyte reaction chamber with the heat         exchanger to affect the desired chemical reactions at the         desired rates following the lowering of the temperature of the         anolyte entering the electrochemical cell. -   13. The apparatus of paragraph 10, wherein:     -   a. the oxidizing species are one or more Type I isopolyanions         (i.e., complex anion redox couple mediators) containing         tungsten, molybdenum, vanadium, niobium, tantalum, or         combinations thereof as addenda atoms in aqueous solution and         the electrolyte is an acid, neutral or alkaline aqueous         solution;     -   b. the oxidizing species are one or more Type I heteropolyanions         formed by incorporation into the aforementioned isopolyanions,         as heteroatoms, any of the elements listed in Table II, either         singly or in combination thereof in the aqueous solutions and         the electrolyte is an acid, neutral, or alkaline aqueous         solution;     -   c. the oxidizing species are one or more of any heteropolyanions         containing at least one heteroatom type (i.e., element)         contained in both Table I and Table II in the aqueous solutions         and the electrolyte is an acid, neutral, or alkaline aqueous         solution;     -   d. the oxidizing species are combinations of anion redox couple         mediators from any or all of the previous four subparagraphs (13         a., 13 b., 13 c., 13 d);     -   e. the oxidizing species are higher valence state of species         found in situ for destroying the infectious waste material; and     -   f. the electrolyte is an acid, neutral, or alkaline aqueous         solution. -   14. The apparatus of paragraph 10, further comprising:     -   a. the aqueous solution is chosen from acids such as but not         limited to nitric acid, sulfuric acid, or phosphoric acid;         alkalines such as but not limited to of sodium hydroxide or         potassium hydroxide; or neutral electrolytes such as but not         limited to sodium or potassium nitrates, sulfates, or         phosphates;     -   b. with an ion-selective or semi-permeable (i.e., microporous         plastic, ceramic, sintered glass frit, etc.) membrane for         separating the anolyte portion and the catholyte portion while         allowing hydrogen or hydronium ion passage from the anolyte to         the catholyte;     -   c. oxidation potentials of redox reactions producing hydrogen         ions are inversely related to pH;     -   d. the infectious waste is liquid waste;     -   e. the infectious waste is solid waste;     -   f. the infectious waste is a combination of liquids and solids         and non-infectious waste; and     -   g. oxidizing species may be interchanged in a preferred         embodiment without changing equipment. -   15. The apparatus of paragraph 10, further comprising:     -   a. a anolyte reaction chamber(s) 5 (b,c) and buffer tank 20         housing the bulk of the anolyte portion and the foraminous EG         Basket 3;     -   a) a anolyte reaction chamber 5 a housing the bulk of the         anolyte portion;     -   b) a anolyte reaction chamber 5 d and buffer tank 20 housing the         bulk of the anolyte portion;     -   c) an input pump 10 is attached to the anolyte reaction chamber         5 a to enter liquid infectious waste into the anolyte reaction         chamber 5 a;     -   d) a spray head 4(a) and a stream head 4(b) attached to the         tubing coming from the electrochemical cell 25 that inputs the         anolyte containing the oxidizer into the anolyte reaction         chamber(s) 5(a,b,c) and buffer tank 20 in such a manner as to         promote mixing of the incoming anolyte with the anolyte already         in the anolyte reaction chambers(s) 5(a,b,c);     -   e) a anolyte reaction chamber(s) 5(b,c) houses a foraminous EG         Basket 3 with a top that holds the contaminated instruments,         equipment, glassware, utensils, and material with the infectious         waste in the electrolyte;     -   f) a hinged lid 1 attached to the anolyte reaction chamber(s)         5(a,b,c) allowing insertion of instruments, equipment,         glassware, utensils, and material into the anolyte portion as         liquid, solid, or a mixture of liquids and solids of infectious         waste;     -   g) the lid 1 contains an locking latch 76 to secure the anolyte         reaction chamber(s) 5(a,b,c) during operation;     -   h) a suction pump 8 is attached to buffer tank 20 to pump         anolyte to the anolyte reaction chamber(s) 5(c,d);     -   i) an input pump 10 to pump anolyte from the anolyte reaction         chamber(s) 5(c,d) back into the buffer tank 20; and     -   k. an air pump 32 to pump off gases from the anolyte reaction         chamber(s) 5(c,d) back into the buffer tank 20 for further         oxidation. -   16. The apparatus of paragraph 10, further comprising:     -   a. an ultraviolet source 11 connected to the anolyte reaction         chamber(s) 5(a,b,c) and buffer tank 20 and decomposing hydrogen         peroxide and ozone into hydroxyl free radicals therein and         increasing efficiency of the MEO process by recovering energy         through the oxidation of the infectious waste materials in the         anolyte chamber by these secondary oxidizers;     -   b. an ultrasonic source 9 connected to the anolyte reaction         chamber(s) 5(a,b,c) and buffer tank 20 for augmenting secondary         oxidation processes by heating the hydrogen peroxide containing         electrolyte to produce extremely short lived and localized         conditions of 4800° C. and 1000 atmospheres pressure within the         anolyte to dissociate hydrogen peroxide into hydroxyl free         radicals thus increasing the oxidation processes;     -   c. an ultrasonic energy 9 source connected into the anolyte         reaction chamber(s) 5(a,b,c) and buffer tank 20 for irradiating         cell membranes in infectious waste materials by momentarily         raising temperature within the cell membranes and causing cell         membrane fail and rupture thus creating greater exposure of cell         contents to oxidizing species in the anolyte;     -   d. the use of ultrasonic energy for mixing material in the         anolyte, via the ultrasonic energy source 9, to induce         microscopic bubble implosion which is used to affect a desired         reduction in sized of the individual second phase infectious         waste volumes and disperse throughout the anolyte;     -   e. a mixer 7 for stirring the anolyte connected to the anolyte         reaction chamber(s) 5(a,b,c) and the buffer tank 20;     -   f. a CO₂ vent 14 for releasing CO₂ atmospherically;     -   g. an inorganic compounds removal and treatment system 15         connected to the anolyte reaction chamber(s) 5(a,b,c) and buffer         tank 20 is used should there be more than trace amount of         chlorine, or other precipitate forming anions present in the         infectious waste being processed, thereby precluding formation         of unstable oxycompounds_(e.g., perchlorates, etc.);     -   h. a gas cleaning system 16 comprises scrubber/absorption         columns;     -   i. the condenser 13 connected to the anolyte reaction chamber(s)         5(a,b,c) and buffer tank 20;     -   j) non-condensable incomplete oxidation products (e.g., low         molecular weight organics, carbon monoxide, etc.) are reduced to         acceptable levels for atmospheric release by a gas cleaning         system 16;     -   k. gas cleaning system 16 is not a necessary component of the         MEO apparatus for the destruction of most types of infectious         waste;     -   l. when the gas cleaning system 16 is incorporated into the MEO         apparatus, the anolyte off-gas is contacted in a gas cleaning         system 16 wherein the non-condensable from the condenser 13 are         introduced into the lower portion of the gas cleaning system 16         through a flow distribution system and a small side stream of         freshly oxidized anolyte direct from the electrochemical cell 25         is introduced into the upper portion of the column, this results         in the gas phase continuously reacting with the oxidizing         mediator species as it rises up the column past the down flowing         anolyte;     -   m. external drain 12, for draining to the organic compound         removal system 17 and the inorganic compounds removal and         treatment system 15, and for draining the anolyte system;     -   n. organic compounds recovery system 17 is used to recover a)         organic materials that are benign and do not need further         treatment, and b) organic materials that is used in the form         they have been reduced and thus would be recovered for that         purpose;     -   o. small thermal control units 21 and 22 are connected to the         flow stream to heat or cool the anolyte to the selected         temperature range;     -   p. anolyte is circulated into the anolyte reaction chamber(s)         5(a,b,c,d) and buffer tank 20 through the electrochemical cell         25 by pump 19 on the anode 26 side of the membrane 27;     -   q. a flush(s) 18 for flushing the anolyte and catholyte systems;     -   r. filter 6 is located at the base of the anolyte reaction         chambers 5(a,b,c,d) and buffer tank 20 to limit the size of the         solid particles to approximately 1 mm in diameter;     -   s. membrane 27 in the electrochemical cell 25 separates the         anolyte portion and catholyte portion of the electrolyte;     -   t. electrochemical cell 25 is energized by a DC power supply 29,         which is powered by the AC power supply 30;     -   u. DC power supply 29 is low voltage high current supply usually         operating below 4V DC but not limited to that range;     -   v. AC power supply 30 operates off a typical 110v AC line for         the smaller units and 240v AC for the larger units;     -   w. electrolyte containment boundary is composed of materials         resistant to the oxidizing electrolyte (e.g., stainless steel,         PTFE, PTFE lined tubing, glass, etc.); and     -   x. an electrochemical cell 25 connected to the anolyte reaction         chamber(s) 5(a,b,c) and buffer tank 20. -   17. The apparatus of paragraph 10, wherein:     -   a. in the anolyte reaction chambers 5(a,b,c) and buffer tank 20         is the aqueous acid, alkali, or neutral salt electrolyte and         mediated oxidizer species solution in which the oxidizer form of         the mediator redox couple initially may be present or may be         generated electrochemically after introduction of the         contaminated instruments, equipment, glassware, utensils, and         materials and application of DC power 29 to the electrochemical         cell 25;     -   b. the contaminated instruments, equipment, glassware, utensils,         and material are introduced when the anolyte is at room         temperature, operating temperature or some optimum intermediate         temperature;     -   c. DC power supply 29 provides direct current to an         electrochemical cell 25;     -   d. pump 19 circulates the anolyte portion of the electrolyte and         the infectious waste material is rapidly oxidized at         temperatures below 100° C. and ambient pressure;     -   e. in-line filter 6 prevents solid particles large enough to         clog the electrochemical cell 25 flow paths from exiting this         reaction chambers 5(a,b,c,d) and buffer tank 20;     -   f. residue is pacified in the form of a salt and may be         periodically removed through the Inorganic Compound Removal and         Treatment System 15 and drain outlets 12;     -   g. electrolyte may be changed through this same plumbing for         introduction into the reaction chambers 5(a,b,c) and buffer tank         20 and 31;     -   h. the process operates at low temperature and ambient         atmospheric pressure and does not generate toxic compounds         during the destruction of the infectious waste, making the         process indoors compatible;     -   i. the system is scalable to a unit large for a large industrial         application; and     -   j. CO₂ oxidation product from the anolyte system A is vented out         the CO₂ vent 14. -   18. The apparatus of paragraph 10, wherein:     -   a. an anolyte recovery system 41 connected to the catholyte pump         (43);     -   b. a thermal control unit 45 connected to the catholyte         reservoir for varying the temperature of the catholyte portion;     -   c. a catholyte reservoir 31 connected to the cathode portion of         the electrochemical cell;     -   d. bulk of the catholyte is resident in the catholyte reaction         chamber 31;     -   e. catholyte portion of the electrolyte flows into a catholyte         reservoir 31;     -   f. an air sparge 37 connected to the catholyte reservoir 31 for         introducing air into the catholyte reservoir 31;     -   g. an anolyte recovery system 41 for capturing the anions and         for reintroducing the anions into the anolyte chamber(s)         5(a,b,c) and buffer tank 20 or disposal from the catholyte         electrolyte;     -   h. an off gas cleaning system 39 for cleaning gases before         release into the atmosphere connected to the catholyte reservoir         31;     -   i. an atmospheric vent 47 for releasing gases into the         atmosphere connected to the off gas cleaning system 39;     -   j. cleaned gas from the off gas cleaning system 39 is combined         with unreacted components of the air introduced into the system         and discharged through the atmospheric vent 47;     -   k. a catholyte reservoir 31 has a screwed top 33 (shown in FIG.         1A), which allow access to the reservoir 31 for cleaning and         maintenance by service personnel;     -   l. a mixer 35 for stirring the catholyte connected to the         catholyte reservoir 31;     -   m. a catholyte pump 43 for circulating catholyte back to the         electrochemical cell 25 connected to the catholyte reservoir 31;     -   n. a drain 12 for draining catholyte;     -   o. a flush 18 for flushing the catholyte system;     -   p. an air sparge 37 connected to the housing for introducing air         into the catholyte reaction chamber 31;     -   q. catholyte portion of the electrolyte is circulated by pump 43         through the electrochemical cell 25 on the cathode 28 side of         the membrane 27;     -   r. small thermal control units 45 and 46 are connected to the         catholyte flow stream to heat or cool the catholyte to the         selected temperature range;     -   s. contact of the oxidizing gas with the catholyte electrolyte         may be enhanced by using conventional techniques for promoting         gas/liquid contact by a ultrasonic vibration 48, mechanical         mixing 35, etc.;     -   t. operating the electrochemical cell 25 at higher than normal         membrane 27 current densities (i.e., above about 0.5 amps/cm²)         will increase the rate of infectious waste destruction, but also         result in increased mediator ion transport through the membrane         into the catholyte;     -   u. optional anolyte recovery system 41 is positioned on the         catholyte side;     -   v. systems using non-nitric acid catholytes may also require air         sparging to dilute and/or remove off-gas such as hydrogen;     -   w. some mediator oxidizer ions may cross the membrane 27 and         this option is available if it is necessary to remove them         through the anolyte recovery system 41 to maintain process         efficiency or cell operability, or their economic worth         necessitates their recovery;     -   x. using the anolyte recovery system 41 the capitol cost of         expanding the size of the electrochemical cell 25 can be         avoided; and     -   y. operating the electrochemical cell 25 at higher than normal         membrane current density (i.e., above about 0.5 amps per         centimeter squared) improves economic efficiency. -   19. The apparatus of paragraph 10, wherein:     -   a. operator runs the MEO Apparatus (FIG. 1A) and FIG. 5(b) by         using the MEO Controller depicted in FIG. 2 MEO Controller;     -   b. controller 49 with microprocessor is connected to a monitor         51 and a keyboard 53;     -   c. operator inputs commands to the controller 49 through the         keyboard 53 responding to the information displayed on the         monitor 51;     -   d. controller 49 runs a program that sequences the steps for the         operation of the MEO apparatus;     -   e. program has pre-programmed sequences of standard operations         that the operator follows or he chooses his own sequences of         operations;     -   f. controller 49 allows the operator to select his own sequences         within limits that assure a safe and reliable operation;     -   g. controller 49 sends digital commands that regulates the         electrical power (AC 30 and DC 29) to the various components in         the MEO apparatus: pumps 19 and 43, mixers 7 and 35, thermal         controls 21, 22, 45, 46, heat exchangers 23 and 24, ultraviolet         sources 11, ultrasonic sources 9 and 48, CO₂ vent 14, air sparge         37, and electrochemical cell 25;     -   h. controller receives component response and status from the         components;     -   i. controller sends digital commands to the sensors to access         sensor information through sensor responses;     -   j. sensors in the MEO apparatus provide digital information on         the state of the various components;     -   k. sensors measure flow rate 59, temperature 61, pH 63, CO₂         venting 65, degree of oxidation 67, air sparge sensor 69, etc;         and     -   l. controller 49 receives status information on the electrical         potential (voltmeter 57) across the electrochemical cell or         individual cells if a multi-cell configuration and between the         anode(s) and reference electrodes internal to the cell(s) 25 and         the current (ammeter 55) flowing between the electrodes within         each cell. -   20. The apparatus of paragraph 10, wherein:     -   a. preferred embodiment, MEO System Model 5.b is sized for use         in a small to mid-size application; other preferred embodiments         have differences in the external configuration and size but are         essentially the same in internal function and components as         depicted in FIGS. 1B, 1D, and 1E;     -   b. preferred embodiment in FIG. 3 comprises a housing 72         constructed of metal or high strength plastic surrounding the         electrochemical cell 25, the electrolyte and the foraminous EG         Basket 3;     -   c. AC power is provided to the AC power supply 30 by the power         cord 78;     -   d. monitor screen 51 is incorporated into the housing 72 for         displaying information about the system and about the         contaminated instruments, equipment, glassware, utensils, and         material being treated;     -   e. control keyboard 53 is incorporated into the housing 72 for         inputting information into the system;     -   f. monitor screen 51 and the control keyboard 53 may be attached         to the system without incorporating them into the housing 72;     -   g. system model 5.b has a control keyboard 53 for input of         commands and data;     -   h. monitor screen 51 to display the systems operation and         functions;     -   i. status lights 73 for on, off and standby, are located above         the keyboard 53 and monitor screen 51;     -   j. in a preferred embodiment, status lights 73 are incorporated         into the housing 72 for displaying information about the status         of the sterilization and/or disinfection of the contaminated         instruments, equipment, glassware, utensils, and materials;     -   k. air sparge 37 is incorporated into the housing 72 to allow         air to be introduced into the catholyte reaction chamber 31         below the surface of the catholyte;     -   l. a CO₂ vent 14 is incorporated into the housing 72 to allow         for CO₂ release from the anolyte reaction chamber housed within;     -   m. in a preferred embodiment, the housing includes means for         cleaning out the MEO infectious waste treatment system,         including a flush(s) 18 and drain(s) 12 through which the         anolyte and catholyte will pass;     -   n. the preferred embodiment further comprises an atmospheric         vent 47 facilitating the releases of gases into the atmosphere         from the catholyte reaction chamber 31;     -   o. hinged lid 1 is opened and the contaminated instruments,         equipment, glassware, utensils, and materials are deposited in         the EG Basket 3 in the chamber 5 b;     -   p. lid stop 2 keeps lid opening controlled; and     -   q. hinged lid 1 is equipped with a locking latch 76 that is         operated by the controller 49. -   21. The apparatus of paragraph 10, wherein:     -   a. MEO apparatus is contained in the housing 72;     -   b. MEO system is started 81 by the operator engaging the ‘ON’         button 74 on the control keyboard 53;     -   c. system controller 49, which contains a microprocessor, runs         the program that controls the entire sequence of operations 82;     -   d. monitor screen 51 displays the steps of the process in the         proper sequence;     -   e. status lights 73 on the panel provide the status of the MEO         apparatus (e.g. on, off, ready, standby);     -   f. lid 1 is opened and the contaminated instruments, equipment,         glassware, utensils, and materials are placed 83 in the anolyte         reaction chamber 5 b in EG Basket 3 as a liquid, solid, or a         mixture of liquids and solids infectious waste, whereupon the         contaminated instruments, equipment, glassware, utensils, and         materials are retained and the liquid infectious waste portion         flows through the EG Basket 3 and into the anolyte;     -   g. locking latch 76 is activated after the contaminated         instruments, equipment, glassware, utensils, and materials are         placed in EG Basket 3;     -   h. pumps 19 and 43 are activated which begins circulation 85 of         the anolyte 87 and catholyte 89, respectively;     -   i. once the electrolyte circulation is established throughout         the system, the mixers 7 and 35 begin to operate 91 and 93;     -   j. depending upon infectious waste characteristics (e.g.,         reaction kinetics, heat of reaction, etc.) it may be desirable         to introduce the contaminated instruments, equipment, glassware,         utensils, and materials into a room temperature or cooler system         with little or none of the mediator redox couple in the oxidizer         form;     -   k. once flow is established the thermal controls units 21, 22,         45, and 46 are turned on 95/97, initiating predetermined anodic         oxidation and electrolyte heating programs;     -   l. the electrochemical cell 25 is energized 94 (by cell commands         56) to the electric potential 57 and current 55 density         determined by the controller program;     -   m. by using programmed electrical power and electrolyte         temperature ramps it is possible to maintain a predetermined         infectious waste destruction rate profile such as a relatively         constant reaction rate as the more reactive infectious waste         components are oxidized, thus resulting in the remaining         infectious waste becoming less and less reactive, thereby         requiring more and more vigorous oxidizing conditions;     -   n. the ultrasonic sources 9 and 48 and ultraviolet systems 11         are activated 99 and 101 in the anolyte reaction chambers         5(a,b,c) and buffer tank 20 and catholyte reaction chamber 31 if         those options are chosen in the controller program;     -   CO₂ vent 14 is activated 103 to release CO₂ from the infectious         waste oxidation process in the anolyte reaction chambers         5(a,b,c) and buffer tank 20;     -   p. air sparge 37 and atmospheric vent 47 are activated 105 in         the catholyte system;     -   q. progress of the destruction process is monitored in the         controller (oxidation sensor 67) by various cell voltages and         currents 55, 57 (e.g., open circuit, anode vs. reference         electrode, ion specific electrodes, etc,) as well as monitoring         CO₂, CO, and O₂ gas 65 composition for CO₂, CO and oxygen         content;     -   r. infectious waste is being decomposed into water and CO₂ the         latter being discharged 103 out of the CO₂ vent 14;     -   s. air sparge 37 draws air 105 into the catholyte reservoir 31,         and excess air is discharged out the atmospheric vent 47;     -   t. when the oxidation sensor 67 determine the desired degree of         infectious waste destruction (sterilization or disinfection) has         been obtained 107, the system goes to standby 109;     -   u. MEO apparatus as an option may be placed in a standby mode         with contaminated instruments, equipment, glassware, utensils,         and materials being added as it is generated throughout the day         and the unit placed in full activation during non-business         hours; and

v. system operator executes system shutdown 111 using the controller keyboard 53. TABLE I SIMPLE ANION REDOX COUPLES MEDIATORS SUB GROUP GROUP ELEMENT VALENCE SPECIES SPECIFIC REDOX COUPLES I A None B Copper (Cu) +2 Cu⁻² (cupric) +2 Species/+3, +4 Species HCuO₂ (bicuprite) +3 Species/+4 Species CuO₂ ⁻² (cuprite) +3 Cu⁺³ CuO₂ ⁻ (cuprate) Cu₂O₃ (sesquioxide) +4 CuO₂ (peroxide) Silver (Ag) +1 Ag⁺ (argentous) +1 Species/+2, +3 Species AgO⁻ (argentite) +2 Species/+3 Species +2 Ag⁻² (argentic) AgO (argentic oxide) +3 AgO⁺ (argentyl) Ag₂O₃ (sesquioxide) Gold (Au) +1 Au⁺ (aurous) +1 Species/+3, +4 Species +3 Au⁺³ (auric) +3 Species/+4 Species AuO⁻ (auryl) H₃AuO₃ ⁻ (auric acid) HAuO₃ ⁻ (monoauarate) HAuO₃ ⁻² (diaurate) AuO₃ ⁻³ (triaurate) Au₂O₃ (auric oxide) Au(OH)₃ (auric hydroxide) +4 AuO₂ (peroxide) II A Magnesium (Mg) +2 Mg⁺² (magnesic) +2 Species/+4 Species +4 MgO₂ (peroxide) Calcium (Ca) +2 Ca⁺² +2 Species/+4 Species +4 CaO₂ (peroxide) Strontium +2 Sr⁺² +2 Species/+4 Species +4 SrO₂ (peroxide) Barium (Ba) +2 Ba⁺² +2 Species/+4 Species +4 BaO₂ (peroxide) II B Zinc (Zn) +2 Zn⁺² (zincic) +2 Species/+4 Species ZnOH⁺ (zincyl) HZnO₂ ⁻ (bizincate) ZnO₂ ⁻² (zincate) +4 ZnO₂ (peroxide) Mercury (Hg) +2 Hg⁺² (mercuric) +2 Species/+4 Species Hg(OH)₂ (mercuric hydroxide) HHgO₂ ⁻ (mercurate) +4 HgO₂ (peroxide) III A Boron +3 H₃BO₃ (orthoboric acid) +3 Species/+4.5, +5 Species H₂BO₃ ⁻, HBO₃ ⁻², BO₃ ⁻³ (orthoborates) BO₂ ⁻ (metaborate) H₂B₄O₇ (tetraboric acid) HB₄O₇ ⁻/B₄O₇ ⁻² (tetraborates) B₂O₄ ⁻² (diborate) B₆O₁₀ ⁻² (hexaborate) +4.5 B₂O₅ ⁻ (diborate) +5 BO₃ ⁻/BO₂ ⁻.H₂ O (perborate) Thallium (TI) +1 TI⁺¹ (thallous) +1 Species/+3 or +3.33 Species +3 TI⁺³ (thallic) +3 Species/+3.33 Species TIO⁺, TIOH⁺², TI(OH)₂ ⁺ (thallyl) TI₂O₃ (sesquioxide) TI(OH)₃ (hydroxide) +3.33 TI₃O₅ (peroxide) B See Rare Earths and Actinides IV A Carbon (C) +4 H₂CO₃ (carbonic acid) +4 Species/+5, +6 Species HCO₃ ⁻ (bicarbonate) CO₃ ⁻² (carbonate) +5 H₂C₂O₆ (perdicarbonic acid) +6 H₂CO₄ (permonocarbonic acid) Germanium (Ge) +4 H₂GeO₃ (germanic acid) +4 Species/+6 Species HGeO₃ ⁻ (bigermaniate) GeO₃ ⁻⁴ (germinate) Ge⁺⁴ (germanic) GeO₄ ⁻⁴ H₂Ge₂O₅ (digermanic acid) H₂Ge₄O₉ (tetragermanic acid) H₂Ge₅O₁₁ (pentagermanic acid) HGe₅O₁₁ ⁻ (bipentagermanate) +6 Ge₅O₁₁ ⁻² (pentagermanate) Tin (Sn) +4 Sn⁺⁴ (stannic) +4 Species/+7 Species HSnO₃ ⁻ (bistannate) SnO₃ ⁻² (stannate) SnO₂ (stannic oxide) Sn(OH)₄ (stannic hydroxide) +7 SnO₄ ⁻ (perstannate) Lead (Pb) +2 Pb⁺² (plumbous) +2, +2.67, +3 Species/+4 Species HPbO₂ ⁻ (biplumbite) PbOH⁺ PbO₂ ⁻² (plumbite) PbO (plumbus oxide) +2.67 Pb₃O₄ (plumbo-plumbic oxide) +3 Pb₂O₃ (sequioxide) A Lead (Pb) +4 Pb⁺⁴ (plumbic) +2, +2.67, +3 Species/+4 Species PbO₃ ⁻² (metaplumbate) HPbO₃ ⁻ (acid metaplumbate) PbO₄ ⁻⁴ (orthoplumbate) PbO₂ (dioxide) B Titanium +4 TiO⁺² (pertitanyl) +4 Species/+6 Species HTiO₄ ⁻ titanate) TiO₂ (dioxide) +6 TiO₂ ⁺² (pertitanyl) HTiO₄ ⁻ (acid pertitanate) TiO₄ ⁻² (pertitanate) TiO₃ (peroxide) Zirconium (Zr) +4 Zr⁺⁴ (zirconic) +4 Species/+5, +6, +7 Species ZrO⁺² (zirconyl) HZrO₃ ⁻ (zirconate) +5 Zr₂O₅ (pentoxide) +6 ZrO₃ (peroxide) +7 Zr₂O₇ (heptoxide) Hafnium (Hf) +4 Hf⁺⁴ (hafnic) +4 Species/+6 Species HfO⁺² (hafnyl) +6 HfO₃ (peroxide) V A Nitrogen +5 HNO₃ (nitric acid) +5 species/+7 Species NO₃ ⁻ (nitrate) +7 HNO₄ (pernitric acid) Phosphorus (P) +5 H₃PO₄ (orthophosphoric acid) +5 Species/+6, +7 species H₂PO₄ ⁻ (monoorthophosphate) HPO₄ ⁻² (diorthophosphate) PO₄ ⁻³ (triorthophosphate) HPO₃ (metaphosphoric acid) H₄P₂O₇ (pryophosphoric acid) H₅P₃O₁₀ (triphosphoric acid) H₆P₄O₁₃ (tetraphosphoric acid) A Phosphorus (P) +6 H₄P₂O₈ (perphosphoric acid) +5 Species/+6, +7 Species +7 H₃PO₅ (monoperphosphoric acid) Arsenic (As) +5 H₃AsO₄ (ortho-arsenic acid) +5 Species/+7 species H₂AsO₄ ⁻ (mono ortho-arsenate) HAsO₄ ⁻² (di-ortho-arsenate) AsO₄ ⁻³ (tri-ortho-arsenate) AsO₂ ⁺ (arsenyl) +7 AsO₃ ⁺ (perarsenyl) Bismuth (Bi) +3 Bi⁺³ (bismuthous) +3 Species/+3.5, +4, +5 Species BiOH⁺² (hydroxybismuthous) BiO⁺ (bismuthyl) BiO₂ ⁻ (metabismuthite) +3.5 Bi₄O₇ (oxide) +4 Bi₂O₄ (tetroxide) +5 BiO₃ ⁻ (metabismuthite) Bi₂O₅ (pentoxide) B Vanadium (V) +5 VO₂ ⁺ (vanadic) +5 Species/+7, +9 Species (See also POM H₃V₂O₇ ⁻ (pyrovanadate) Complex Anion H₂VO₄ ⁻ (orthovanadate) Mediators) VO₃ ⁻ (metavanadate) HVO₄ ⁻² (orthovanadate) VO₄ ⁻³ (orthovanadate) V₂O₅ (pentoxide) H₄V₂O₇ (pyrovanadic acid) HVO₃ (metavanadic acid) H₄V₆O₁₇ (hexavanadic acid) +7 VO₄ ⁻ (pervanadate) +9 VO₅ ⁻ (hypervanadate) VI B Chromium +3 Cr⁺³ (chromic) +3 Species/+4, +6 Species CrOH⁺², Cr(OH)₂ ⁺ (chromyls) +4 Species/+6 Species CrO₂ ⁻, CrO₃ ⁻³ (chromiles) Cr₂O₃ (chromic oxide) Cr(OH)₃ (chromic hydroxide) +4 CrO₂ (dioxide) Cr(OH)₄ (hydroxide) +6 H₂CrO₄ (chromic acid) HCrO₄ ⁻ (acid chromate) CrO₄ ⁻² (chromate) Cr₂O₇ ⁻² (dichromate) Molybdenum (Mo) +6 HMoO₄ ⁻ (bimolybhate) +6 Species/+7 Species (See also POM MoO₄ ⁻² (molydbate) Complex Anion MoO₃ (molybdic trioxide) Mediators) H₂MoO₄ (molybolic acid) +7 MoO₄ ⁻ (permolybdate) Tungsten (W) +6 WO₄ ⁻² (tungstic) +6 Species/+8 Species (See also POM WO₃ (trioxide) Complex Anion H₂WO₄ (tungstic acid) Mediators) +8 WO₅ ⁻² (pertungstic) H₂WO₅ (pertungstic acid) VII A Chlorine (Cl) −1 Cl⁻ (chloride) −1 Species/+1, +3, +5, +7 Species +1 HClO (hypochlorous acid) +1 Species/+3, +5, +7 Species ClO⁻ (hypochlorite) +3 Species/+5, +7 Species +3 HClO₂ (chlorous acid) +5 Species/+7 Species ClO₂ ⁻ (chlorite) +5 HClO₃ (chloric acid) ClO₃ ⁻ (chlorate) +7 HClO₄ (perchloric acid) ClO₄ ⁻, HClO₅ ⁻², ClO₅ ⁻³, Cl₂O₉ ⁻⁴ (perchlorates) V B Niobium (Nb) +5 NbO₃ ⁻ (metaniobate) +5 Species/+7 species (See also POM NbO₄ ⁻³ (orthoniobate) Complex Anion Nb₂O₅ (pentoxide) Mediators) HNbO₃ (niobid acid) +7 NbO₄ ⁻ (perniobate) Nb₂O₇ (perniobic oxide) HNbO₄ (perniobic acid) Tantalum (Ta) +5 TaO₃ ⁻ (metatantalate) +5 species/+7 species (See also POM TaO₄ ⁻³ (orthotanatalate) Complex Anion Ta₂O₅ (pentoxide) Mediators) HTaO₃ (tantalic acid) +7 TaO₄ ⁻ (pentantalate) Ta₂O₇ (pertantalate) HTaO₄.H₂O (pertantalic acid) VI A Sulfur (S) +6 H₂SO₄ (sulfuric acid) +6 Species/+7, +8 Species HSO₄ ⁻ (bisulfate) SO₄ ⁻² (sulfate) +7 S₂O₈ ⁻² (dipersulfate) +8 H₂SO₅ (momopersulfuric acid) Selenium (Se) +6 H₂Se₂O₄ (selenic acid) +6 species/+7 Species HSeO₄ ⁻ (biselenate) SeO₄ ⁻² (selenate) +7 H₂Se₂O₈ (perdiselenic acid) Tellurium (Te) +6 H₂TeO₄ (telluric acid) +6 species/+7 species HTeO₄ ⁻ (bitellurate) TeO₄ ⁻² (tellurate) +7 H₂Te₂O₈ (perditellenic acid) Polonium (Po) +2 Po⁺² (polonous) +2, +4 species/+6 Species +4 PoO₃ ⁻² (polonate) +6 PoO₃ (peroxide) VII A Bromine (Br) −1 Br⁻ (bromide) −1 Species/+1, +3, +5, +7 Species +1 HBrO (hypobromous acid) +1 Species/+3, +5, +7 Species BrO⁻ (hypobromitee) +3 Species/+5, +7 Species +3 HBrO₂ (bromous acid) +5 Species/+7 Species BrO2⁻ (bromite) +5 HBrO₃ (bromic acid) BrO₃ ⁻ (bromate) +7 HBrO₄ (perbromic acid) BrO₄ ⁻, HBrO₅ ⁻², BrO₅ ⁻³, Br₂O₉ ⁻⁴ (prebromates) Iodine −1 I⁻ (iodide) −1 Species/+1, +3, +5, +7 Species +1 HIO (hypoiodus acid) +3 Species/+3, +5, +7 Species IO⁻ (hypoiodite) +3 Species/+5, +7 Species +3 HIO₂ (iodous acid) +5 Species/+7 Species IO₂ ⁻ (iodite) +5 HIO₃ (iodic acid) IO₃ ⁻ (iodate) +7 HIO₄ (periodic acid) IO₄ ⁻, HIO₅ ⁻², IO₅ ⁻³, I₂O₉ ⁻⁴ (periodates) B Manganese (Mn) +2 Mn⁺² (manganeous) +2 Species/+3, +4, +6, +7 Species HMnO₂ ⁻ (dimanganite) +3 Species/+4, +6, +7 Species +3 Mn⁺³ (manganic) +4 Species/+6, +7 Species +4 MnO₂ (dioxide) +6 Species/+7 Species +6 MnO₄ ⁻² (manganate) +7 MnO₄ ⁻ (permanganate) VIII Period 4 Iron (Fe) +2 Fe⁺² (ferrous) +2 Species/+3, +4, +5, +6 Species HFeO₂ ⁻ (dihypoferrite) +3 Species/+4, +5, +6 Species +3 Fe⁺³, FeOH⁺², Fe(OH)₂ ⁺ (ferric) +4 Species/+5, +6 Species FeO₂ ⁻ (ferrite) +5 Species/+6 Species +4 FeO⁺² (ferryl) FeO₂ ⁻² (perferrite) +5 FeO₂ ⁺ (perferryl) +6 FeO₄ ⁻² (ferrate) Cobalt (Co) +2 Co⁺² (cobalous) +2 Species/+3, +4 Species HCoO₂ ⁻ (dicobaltite) +3 Species/+4 Species +3 Co⁺³ (cobaltic) Co₂O₃ (cobaltic oxide) +4 CoO₂ (peroxide) H₂CoO₃ (cobaltic acid) Nickel (Ni) +2 Ni⁺² (nickelous) +2 Species/+3, +4, +6 Species NiOH⁺ +3 Species/+4, +6 Species HNiO₂ ⁻ (dinickelite) +4 Species/+6 Species NiO₂ ⁻² (nickelite) +3 Ni⁺³ (nickelic) Ni₂O₃ (nickelic oxide) +4 NiO₂ (peroxide) +6 NiO₄ ⁻² (nickelate) Period 5 Ruthenium (Ru) +2 Ru⁺² +2 Species/+3, +4, +5, +6, +7, +8 Species +3 Ru⁺³ +3 Species/+4, +5, +6, +7, +8 Species Ru₂O₃ (sesquioxide) +4 Species/+5, +6, +7, +8 Species Ru(OH)₃ (hydroxide) +5 Species/+6, +7, +8 Species +4 Ru⁺⁴ (ruthenic) +6 Species/+7, +8 Species RuO₂ (ruthenic dioxide) +7 Species/+8 Species Ru(OH)₄ (ruthenic hydroxide) +5 Ru₂O₅ (pentoxide) +6 RuO₄ ⁻² (ruthenate) RuO₂ ⁺² (ruthenyl) RuO₃ (trioxide) +7 RuO₄ ⁻ (perruthenate) +8 H₂RuO₄ (hyperuthenic acid) HRuO₅ ⁻ (diperruthenate) RuO₄ (ruthenium tetroxide) Rhodium (Rh) +1 Rh⁺ (hyporhodous) +1 Species/+2, +3, +4, +6 Species +2 Rh⁺² (rhodous) +2 Species/+3, +4, +6 Species +3 Rh⁺³ (rhodic) +3 Species/+4, +6 Species Rh₂O₃ (sesquioxide) +4 Species/+6 Species +4 RhO₂ (rhodic oxide) Rh(OH)₄ (hydroxide) +6 RhO₄ ⁻² (rhodate) RhO₃ (trioxide) Palladium +2 Pd⁺² (palladous) +2 Species/+3, +4, +6 Species PdO₂ ⁻² (palladite) +3 Species/+4, +6 Species +3 Pd₂O₃ (sesquioxide) +4 Species/+6 Species +4 PdO₃ ⁻² (palladate) PdO₂ (dioxide) Pd(OH)₄ (hydroxide) +6 PdO₃ (peroxide) Period 6 Iridium (Ir) +3 Ir⁺³ (iridic) +3 Species/+4, +6 Species Ir₂O₃ (iridium sesquioxide) +4 Species/+6 Species Ir (OH)₃ (iridium hydroxide) +4 IrO₂ (iridic oxide) Ir (OH)₄ (iridic hydroxide) +6 IrO₄ ⁻² (iridate) IrO₃ (iridium peroxide) Platinum (Pt) +2 Pt⁺² (platinous) +2, +3 Species/+4, +6 Species +3 Pt₂O₃ (sesquioxide) +4 Species/+6 Species +4 PtO₃ ⁻² (palatinate) PtO⁺² (platinyl) Pt(OH)⁺³ PtO₂ (platonic oxide) IIIB Rare Cerium (Ce) +3 Ce⁺³ (cerous) +3 Species/+4, +6 Species earths Ce₂O₃ (cerous oxide) +4 Species/+6 Species Ce(OH)₃ (cerous hydroxide) +4 Ce⁺⁴, Ce(OH)⁺³, Ce(OH)₂ ⁻², Ce(OH)₃ ⁺ (ceric) CeO₂ (ceric oxide) +6 CeO₃ (peroxide) Praseodymium (Pr) +3 Pr⁺³ (praseodymous) +3 species/+4 species Pr₂O₃ (sesquioxide) Pr(OH)₃ (hydroxide) +4 Pr⁺⁴ (praseodymic) PrO₂ (dioxide) Neodymium +3 Nd⁺³ +3 Species/+4 Species Nd₂O₃ (sesquioxide) +4 NdO₂ (peroxide) Terbium (Tb) +3 Tb⁺³ +3 Species/+4 Species Tb₂O₃ (sesquioxide) +4 TbO₂ (peroxide) Actinides Thorium (Th) +4 Th⁺⁴ (thoric) +4 Species/+6 Species ThO⁺² (thoryl) HThO₃ ⁻ (thorate) +6 ThO₃ (acid peroxide) Uranium (U) +6 UO₂ ⁺² (uranyl) +6 Species/+8 Species UO₃ (uranic oxide) +8 HUO₅ ⁻, UO₅ ⁻² (peruranates) UO₄ (peroxide) Neptunium (Np) +5 NpO₂ ⁺ (hyponeptunyl) +5 Species/+6, +8 Species Np₂O₅ (pentoxide) +6 Species/+8 Species +6 NpO₂ ⁺² (neptunyl) NpO₃ (trioxide) +8 NpO₄ (peroxide) Plutonium (Pu) +3 Pu⁺³ (hypoplutonous) +3 Species/+4, +5, +6 Species +4 Pu⁺⁴ (plutonous) +4 Species/+5, +6 Species PuO₂ (dioxide) +5 Species/+6 Species +5 PuO₂ ⁺ (hypoplutonyl) Pu₂O₅ (pentoxide) +6 PuO₂ ⁺² (plutonyl) PuO₃ (peroxide) Americium (Am) +3 Am⁺³ (hypoamericious) +4 Am⁺⁴ (americous) AmO₂ (dioxide) Am(OH)₄ (hydroxide) +5 AmO₂ ⁺ (hypoamericyl) Am₂O₅ (pentoxide) +6 AmO₂ ⁺² (americyl) AmO₃ (peroxide)

TABLE II ELEMENTS PARTICIPATING AS HETEROATOMS IN HETEROPOLYANION COMPLEX ANION REDOX COUPLE MEDIATORS GROUP SUB GROUP ELEMENT I A Lithium (Li), Sodium (Na), Potassium (K), and Cesium (Cs) B Copper (Cu), Silver (Ag), and Gold (Au) II A Beryllium (Be), Magnesium (Mg), Calcium (Ca), Strontium (Sr), and Barium (Ba) B Zinc (Zn), Cadmium (Cd), and Mercury (Hg) III A Boron (B), and Aluminum (Al) B Scandium (Sc), and Yttrium (Y) - (See Rare Earths) IV A Carbon (C), Silicon (Si), Germanium (Ge), Tin (Sn) and Lead (Pb) B Titanium (Ti), Zirconium (Zr), and Hafnium (Hf) V A Nitrogen (N), Phosphorous (P), Arsenic (As), Antimony (Sb), and Bismuth (Bi) B Vanadium (V), Niobium (Nb), and Tantalum (Ta) VI A Sulfur (S), Selenium (Se), and Tellurium (Te) B Chromium (Cr), Molybdenum (Mo), and Tungsten (W) VII A Fluorine (F), Chlorine (Cl), Bromine (Br), and Iodine (I) B Manganese (Mn), Technetium (Tc), and Rhenium (Re) VIII Period 4 Iron (Fe), Cobalt (Co), and Nickel (Ni) Period 5 Ruthenium (Ru), Rhodium (Rh), and Palladium (Pd) Period 6 Osmium (Os), Iridium (Ir), and Platinum (Pt) IIIB Rare Earths All 

1. A process for sterilizing/disinfecting by treating and oxidizing infectious waste materials on the contaminated instruments, equipment, glassware, utensils, and/or infectious waste materials comprising disposing an electrolyte in an electrochemical cell, separating the electrolyte into an anolyte portion and a catholyte portion with an ion-selective membrane or semipermeable membrane applying a direct current voltage between the anolyte portion and the catholyte portion, placing the contaminated instruments, equipment, glassware, utensils, and/or infectious waste materials in the anolyte portion, and oxidizing the infectious waste materials in the anolyte portion with a mediated electrochemical oxidation (MEO) process, wherein the anolyte portion further comprises a mediator in aqueous solution and the electrolyte is an acid, neutral or alkaline aqueous solution.
 2. The process of claim 1, wherein the mediator is selected from the group of mediators described in Table I.
 3. The process of claim 1, wherein the oxidizing species are selected from one or more of a group of Type I complex anion redox couple isopolyanion mediators containing tungsten, molybdenum, vanadium, niobium, tantalum, or combinations thereof as addenda atoms in aqueous solution.
 4. The process of claim 1, wherein the oxidizing species are selected from one or more of a group of Type I heteropolyanions formed by incorporation into Type I isopolyanions, as heteroatoms, any of the elements listed in Table II, either singly or in combination thereof in the aqueous solution.
 5. The process of claim 1, wherein the oxidizing species are selected from one or more of a group of heteropolyanions containing at least one heteroatom type element contained in both Table I and Table II in the aqueous solution.
 6. The process of claim 1, wherein the oxidizing species are selected from a group of combinations of anion redox couple mediators described in Tables I and II, and wherein reduced forms of the redox couples are reoxidized in the anolyte portion within the electrochemical cell.
 7. The process of claim 1, further comprising introducing catalyst additives to the electrolyte and thereby contributing to kinetics of the mediated electrochemical processes while keeping the additives from becoming directly involved in the oxidizing of the infectious waste materials.
 8. The process of claim 1, further comprising adding stabilizing compounds to the electrolyte for overcoming and stabilizing the short lifetime of oxidized forms of higher oxidation state species of the mediator.
 9. The process of claim 1, wherein the oxidizing species are identified in Table I, and wherein each of the species has normal valence states and higher valence oxidizing states and further comprising creating the higher valence oxidizing states of the oxidizing species by stripping electrons from normal valence state species in the electrochemical cell.
 10. The process of claim 1, wherein the oxidizing species are super oxidizers which exhibit oxidation potentials of at least 1.7 volts at 1 molar, 25° C. and pHl and which are redox couple species that have the capability of producing free radicals of hydroxyl or perhydroxyl, and further comprising creating free radical secondary oxidizers by reacting the super oxidizers with water.
 11. The process of claim 1, further comprising using an alkaline solution, aiding decomposing of the biological materials derived from base promoted ester hydrolysis, saponification, of fatty acids, and forming water soluble alkali metal salts of the fatty acids and glycerin in a process similar to the production of soap from animal fat by introducing it into a hot aqueous lye solution.
 12. The process of claim 1, further comprising using an alkaline anolyte solution for absorbing CO₂ from the oxidizing of the infectious waste materials and forming bicarbonate/carbonate solutions, which subsequently circulate through the electrochemical cell, producing percarbonate oxidizers.
 13. The process of claim 1, wherein the oxidizing agents are super oxidizers, and further comprising generating inorganic free radicals in aqueous solutions from carbonate, azide, nitrite, nitrate, phosphite, phosphate, sulfite, sulfate, selenite, thiocyanate, chloride, bromide, iodide, and formate oxidizing species.
 14. The process of claim 1, wherein the membrane is microporous plastic, ion-selective, porous ceramic or sintered glass frit.
 15. The process of claim 1, further comprising impressing an AC voltage upon the direct current voltage for retarding formation of cell performance limiting surface films on the electrode.
 16. The process of claim 1, further comprising disposing a foraminous basket in the anolyte and holding the infectious waste materials in the basket.
 17. The process of claim 1, wherein the catholyte contains HNO₃ or NO₃ ⁻ salts, and further comprising adding oxygen to the catholyte portion.
 18. The process of claim 1, wherein the mediator is simple anions described in Table I, Type I isopolyanions containing tungsten, molybdenum, vanadium, niobium, tantalum, or combinations thereof as addenda atoms; Type I heteropolyanions formed by incorporation into the aforementioned isopolyanions, as heteroatoms, any of the elements listed in Table II, either singly or in combinations thereof; or any heteropolyanions containing at least one heteroatom type contained in both Table I and Table II.
 19. The process of claim 1, further comprising adjusting temperature between 0° C. and temperature of the anolyte portion before it enters the electrochemical cell for enhancing generation of oxidized forms of the mediator, and adjusting the temperature between 0° C. and below the boiling temperature of the anolyte portion entering the anolyte reaction chamber affecting desired chemical reactions at desired rates.
 20. The process of claim 1, further comprising introducing an ultrasonic energy into the anolyte portion, rupturing cell membranes in the infectious waste materials by momentarily raising local temperature within the cell membranes with the ultrasonic energy to above several thousand degrees, and causing cell membrane failure.
 21. The process of claim 1, further comprising the evolving of oxygen from the anode is feed to a hydrogen fuel apparatus to increase the percentage oxygen available from the ambient air.
 22. The process of claim 1, further comprising introducing ultraviolet energy into the anolyte portion and decomposing hydrogen peroxide and ozone into hydroxyl free radicals therein, thereby increasing efficiency of the process by converting products of electron consuming parasitic reactions, ozone and hydrogen peroxide, into viable free radical secondary oxidizers without consumption of additional electrons.
 23. The process of claim 1, further comprising adding a surfactant to the anolyte portion for promoting dispersion of the infectious waste materials or intermediate stage reaction products within the aqueous solution when the infectious waste materials or reaction products are not water-soluble and tend to form immiscible layers.
 24. The process of claim 1, further comprising attacking specific organic molecules with the oxidizing species while operating at low temperatures and preventing formation of dioxins and furans.
 25. The process of claim 1, further comprising breaking down the infectious waste materials into organic compounds and attacking the organic compounds using as the mediator simple and/or complex anion redox couple mediators or inorganic free radicals and generating organic free radicals.
 26. The process of claim 1, wherein the treating and oxidizing infectious waste material comprises treating and oxidizing infectious waste.
 27. The process of claim 1, further comprising raising normal valence state mediator anions to a higher valence state by stripping the mediator anions of electrons in the electrochemical cell, wherein oxidized forms of weaker redox couples present in the mediator are produced by similar anodic oxidation or reaction with oxidized forms of stronger redox couples present and the oxidized species of the redox couples oxidize molecules of the infectious waste materials and are themselves converted to their reduced form, whereupon they are oxidized by the aforementioned mechanisms and the redox cycle continues.
 28. A process for treating and oxidizing infectious waste, comprising circulating anions of mediator oxidizing species in an electrolyte through an electrochemical cell and affecting anodic oxidation of reduced forms of reversible redox couples into oxidized forms, contacting the anions with the infectious waste in an anolyte portion of the electrolyte in a primary oxidation process, involving super oxidizer anions, having an oxidation potential above a threshold value of 1.7 volts at 1 molar, 25° C. and pHl are present there is a free radical oxidizer driven secondary oxidation process, adding energy from an energy source to the anolyte portion and augmenting the secondary oxidation processes, breaking down hydrogen peroxide and ozone in the anolyte portion into hydroxyl free radicals, and increasing an oxidizing effect of the secondary oxidation processes.
 29. The process of claim 28, wherein the adding energy comprises irradiating the anolyte portion with ultraviolet energy.
 30. The process of claim 28, wherein the adding energy comprises introducing an ultrasonic energy source into the anolyte portion, irradiating cell membranes in the infectious waste, momentarily raising local temperature within the cell membranes, causing cell membrane failure, and creating greater exposure of cell contents to oxidizing species in the anolyte portion.
 31. The process of claim 28, wherein the mediator oxidizing species are simple anions redox couple mediators described in Table I; Type I isopolyanions formed by Mo, W, V, Nb, Ta, or mixtures thereof; Type I heteropolyanions formed by incorporation into the isopolyanions if any of the elements listed in Table II (heteroatoms) either singly or in thereof, or heteropolyanions containing at least one heteroatom type element contained in both Table I and Table II or combinations of the mediator oxidizing species from any or all of these generic groups.
 32. The process of claim 28, further comprising using oxidizer species that are found in situ in the infectious waste to be decomposed, by circulating the infectious waste-anolyte mixture through the electrochemical cell where in an oxidized form of an in situ reversible redox couple is formed by anodic oxidizing or reacting with an oxidized form of a more powerful redox couple added to the anolyte and anodically oxidized in the electrochemical cell, thereby destroying the infectious waste material.
 33. The process of claim 28, further comprising using an alkaline electrolyte selected from a group consisting of NaOH or KOH and combinations thereof, with the mediator oxidizing species, wherein a reduced form of a mediator redox couple has sufficient solubility in said electrolyte for allowing desired oxidation of the infectious waste material.
 34. The process of claim 28, wherein the oxidation potential of redox reactions of the mediator oxidizing species and infectious waste molecules producing hydrogen ions are inversely proportional to electrolyte pH, and thus with a selection of a mediator redox couple increasing the electrolyte pH reduces the electric potential required, thereby reducing electric power consumed per unit mass of infectious waste destroyed.
 35. The process of claim 28, wherein the electrolyte is an aqueous solution chosen from acids, alkalines and neutral electrolytes and mixtures thereof.
 36. The process of claim 28, wherein the adding energy comprises using ultrasonic energy and inducing microscopic bubble expansion and implosion for reducing size of infectious waste volumes dispersed in the anolyte.
 37. The process of claim 28, further comprising interchanging the mediator oxidizing species without changing equipment, and wherein the electrolyte is an acid, neutral or alkaline aqueous solution.
 38. The process of claim 28, wherein the treating and oxidizing infectious waste comprises treating and oxidizing infectious waste from military ships, submarines, destroyers, cruisers and carriers.
 39. The process of claim 28, wherein the treating and oxidizing infectious waste comprises treating and oxidizing infectious waste from commercial ships, cruise ships, tankers, cargo ships, fishing boats, recreational craft and houseboats.
 40. The process of claim 28, further comprising separating the anolyte portion and a catholyte portion of the electrolyte with a hydrogen or hydronium ion-permeable membrane, microporous polymer, porous ceramic or glass frit membrane.
 41. The process of claim 28, further comprising electrically energizing the electrochemical cell at a potential level sufficient for forming the oxidized forms of redox couples having highest oxidizing potential in the anolyte, introducing contaminated instruments, equipment, glassware, utensils, and infectious waste materials into the anolyte portion, forming reduced forms of one or more reversible redox couples by contacting with oxidizable molecules, the reaction with which oxidizes the oxidizable material with the concomitant reduction of the oxidized form of the reversible redox couples to their reduced form, and wherein the adding energy comprises providing an ultrasonic source connected to the anolyte for augmenting secondary oxidation processes by momentarily heating the hydrogen peroxide in the electrolyte to 4800° C. at 1000 atmospheres thereby dissociating the hydrogen peroxide into hydroxyl free radicals thus increasing the oxidizing processes.
 42. The process of claim 41, further comprising oxidation potentials of redox reactions producing hydrogen ions are inversely related to pH;
 43. The process of claim 28, wherein the process is performed at a temperature from slightly above 0° C. to slightly below the boiling point of the electrolyte.
 44. The process of claim 43, wherein the temperature at which the process is performed is varied.
 45. The process of claim 28, wherein the sterilizing and disinfecting contaminated instruments, equipment, glassware, utensils, and infectious waste materials comprises treating and oxidizing solid infectious waste.
 46. The process of claim 28, wherein the sterilizing and disinfecting contaminated instruments, equipment, glassware, utensils, and infectious waste materials comprises treating and oxidizing liquid infectious waste.
 47. The process of claim 28, wherein the sterilizing and disinfecting contaminated instruments, equipment, glassware, utensils, and infectious waste materials comprises treating and oxidizing a combination of solid and liquid infectious waste.
 48. The process of claim 28, further comprising requiring removing and treating precipitates resulting from combinations of the oxidizing species and other species released from the infectious waste during destruction.
 49. The process of claim 28, further comprising a catholyte portion of the electrolyte, and wherein the anolyte and catholyte portions of electrolyte are independent of one another, and comprise aqueous solutions of acids, alkali or neutral salt.
 50. The process of claim 28, further comprising separating a catholyte portion of the electrolyte from the anolyte portion with a membrane, operating the electrochemical cell at a current density greater then 0.5 amp per square centimeter across the membrane, and near a limit over which there is the possibility that metallic anions may leak through the membrane in small quantities, and recovering the metallic anions through a resin column, thus allowing a greater rate of destruction of infectious waste materials in the anolyte portion.
 51. The process of claim 28, wherein the catholyte solution further comprises an aqueous solution and the electrolyte in the solution is composed of acids, alkali or neutral salts of strong acids and bases, and further comprising adding oxygen to this solution when HNO₃ or NO₃ ⁻ can occur in the catholyte, controlling concentration of electrolyte in the catholyte to maintain conductivity of the catholyte portion desired in the electrochemical cell, providing mechanical mixing and/or ultrasonic energy induced microscopic bubble formation, and implosion for vigorous mixing in the catholyte solution for oxidizing the nitrous acid and small amounts of nitrogen oxides NO_(x), introducing air into the catholyte portion for promoting the oxidizing of the nitrous acid and the small amounts of NO_(x), and diluting any hydrogen produced in the catholyte portion before releasing the air and hydrogen.
 52. The process of claim 28, further comprising the evolving of hydrogen is feed to an apparatus that use hydrogen as a fuel (e.g., a fuel cell or an hydrogen burner).
 53. Apparatus for treating and oxidizing infectious waste materials comprising an electrochemical cell, an aqueous electrolyte disposed in the electrochemical cell, a hydrogen or hydronium ion-permeable or selective membrane, disposed in the electrochemical cell for separating the cell into anolyte and catholyte chambers and separating the electrolyte into aqueous anolyte and catholyte portions, electrodes further comprising an anode and a cathode disposed in the electrochemical cell respectively in the anolyte and catholyte chambers and in the anolyte and catholyte portions of the electrolyte, a power supply connected to the anode and the cathode for applying a direct current voltage between the anolyte and the catholyte portions of the electrolyte, and oxidizing of the infectious waste materials in the anolyte portion with a mediated electrochemical oxidation (MEO) process wherein the anolyte portion further comprises a mediator in aqueous solution for producing reversible redox couples used as oxidizing species and the electrolyte is an acid, neutral or alkaline aqueous solution.
 54. The apparatus of claim 53, further comprising an anolyte reaction chamber and buffer tank housing the bulk of the anolyte solution, an input pump to enter liquid infectious waste into the anolyte reaction chamber, a spray head and stream head to introduce the anolyte from the electrochemical cell into the anolyte reaction chamber in such a manner as to promote mixing of the incoming anolyte and the anolyte mixture in the anolyte reaction chamber, a hinged lib to allow insertion of infectious waste into the anolyte portion as liquid, solid of combination of both, a locking latch to secure the lid during operation of the system, a suction pump attached to the buffer tank to pump anolyte from the buffer tank to the anolyte reaction chamber, a input pump to pump anolyte from the anolyte reaction chamber back to the buffer tank, and an air pump to pump off gases from the anolyte reaction chamber back to the buffer tank for further oxidation.
 55. The apparatus of claim 53, further comprising a foraminous basket disposed in the anolyte chamber for receiving the infectious waste materials.
 56. The apparatus of claim 53, further comprising additives disposed in the electrolyte for contributing to kinetics of the mediated electrochemical processes while keeping it from becoming directly involved in the oxidizing of the infectious waste materials, and stabilizer compounds disposed in the electrolyte for stabilizing higher oxidation state species of oxidized forms of the reversible redox couples used as the oxidizing species in the electrolyte.
 57. The apparatus of claim 53, wherein the oxidizer species are simple anions redox couple mediators described in Table I Type I isopolyanions formed by Mo, W, V, Nb, Ta, or mixtures there of, Type I heteropolyanions formed by incorporation into the isopolyanions in heteroatom elements listed in Table II, or any heteropolyanions containing at least one heteroatom type element contained in both Table I and Table II or combinations of mediator species from any or all of these generic groups.
 58. The apparatus of claim 53, wherein the oxidizing species are super oxidizers and further comprising creating secondary oxidizers disposed in the anolyte portion by reacting with the super oxidizers in the aqueous anolyte.
 59. The apparatus of claim 53, wherein the anolyte portion comprises an alkaline solution for aiding decomposing the infectious waste materials, for absorbing CO₂, for forming alkali metal bicarbonate/carbonate for circulating through the electrochemical cell, and for producing a percarbonate oxidizer.
 60. The apparatus of claim 53, wherein the anolyte portion further comprises super oxidizers generating inorganic free radicals in aqueous solutions derived from carbonate, azide, nitrite, nitrate, phosphite, phosphate, sulfite, sulfate, selenite, thiocyanate, chloride, bromide, and iodide species, anions with an oxidation potential above a threshold value of 1.7 volts at 1 molar, 25° C. and pHl (i.e., super oxidizer) for involving in a secondary oxidation process for producing oxidizers, and organic free radicals for aiding the process and breaking down the infectious waste materials into simpler smaller molecular structure organic compounds.
 61. The apparatus of claim 53, further comprising an ultrasonic energy source within or near the anolyte chamber for producing microscopic bubbles and implosions for reducing in size individual second phase waste volumes dispersed in the anolyte.
 62. The apparatus of claim 53, wherein the membrane is made of microporous polymer, porous ceramic or glass frit.
 63. The apparatus of claim 53, further comprising an AC source for impression of an AC voltage upon the DC voltage to retard the formation of cell performance limiting surface films on the electrodes.
 64. The apparatus of claim 53, further comprising an air sparge connected to the catholyte reservoir, whereby oxygen contained in the air oxidizes nitrous acid and the small amounts of nitrogen oxides (NO_(x)), produced by cathode reactions when HNO₃ or NO₃ ⁻ salts are present in the catholyte.
 65. The apparatus of claim 53, wherein each of the oxidizing species has normal valence states in reduced forms of redox couples and higher valence oxidizing states oxidized forms of redox couples of the oxidizing species created by stripping and reducing electrons off normal valence state species in the electrochemical cell.
 66. The apparatus of claim 53, wherein the anolyte portions are alkaline solutions and oxidation potentials of redox reactions producing hydrogen ions are inversely related to pH, which reduces the electrical power required to destroy the infectious waste.
 67. The apparatus of claim 53, wherein the oxidizing species attack specific organic molecules while operating at temperatures sufficiently low so as to preventing the formation of dioxins and furans.
 68. The apparatus of claim 53, wherein the power supply energizes the electrochemical cell at a potential level sufficient to form the oxidized form of the redox couple having the highest oxidation potential in the anolyte, and further comprising a heat exchanger connected to the anolyte chamber for controlling temperature between 0° C. and slightly below the boiling temperature of the anolyte with the heat exchanger before the anolyte enters the electrochemical cell enhancing the generation of oxidized forms of the anion redox couple mediator, and adjusting the temperature of the anolyte to the range between 0° C. and slightly below the boiling temperature when entering the anolyte reaction chamber.
 69. The apparatus of claim 53, wherein the oxidizing species are one or more Type I isopolyanion complex anion redox couple mediators containing tungsten, molybdenum, vanadium, niobium, tantalum, or combinations thereof as addenda atoms in aqueous solution;
 70. The apparatus of claim 69, wherein the oxidizing species are one or more Type I heteropolyanions formed by incorporation into the isopolyanions, as heteroatoms, of the elements listed in Table II, either singly or in combination thereof.
 71. The apparatus of claim 53, wherein the oxidizing species are one or more heteropolyanions containing at least one heteroatom type element contained in Table I and Table II.
 72. The apparatus of claim 53, wherein the oxidizing species are higher valence state of species found in situ for destroying the infectious waste material.
 73. The apparatus of claim 53, wherein the infectious waste material is pharmaceutical manufacturing process waste abatement, obsolete pharmaceuticals, or infectious waste from military ships or commercial ships.
 74. The apparatus of claim 53, wherein the membrane is hydrogen or hydronium ion semi permeable or ion-selective, microporous polymer, porous ceramic or glass frit membrane for separating the anolyte portion and the catholyte portion while allowing hydrogen or hydronium ion passage from the anolyte to the catholyte.
 75. The apparatus of claim 53, wherein oxidation potentials of redox reactions producing hydrogen ions are inversely related to pH, the infectious waste is liquid or solid, or a combination of liquids and solids, and the oxidizing species are interchangeable without changing other elements of the apparatus.
 76. The apparatus of claim 53, further comprising an ultraviolet source connected to the anolyte chamber for decomposing hydrogen peroxide and ozone into hydroxyl free radicals as secondary oxidizers and increasing efficiency of the process by recovering energy through the oxidation of the infectious waste materials in the anolyte chamber by the secondary oxidizers.
 77. The apparatus of claim 53, further comprising an ultrasonic source connected to the anolyte for augmenting secondary oxidation processes by heating hydrogen peroxide containing electrolyte to 4800° C., at 1000 atmospheres for dissociating hydrogen peroxide into hydroxyl free radicals and thus increasing concentration of oxidizing species and rate of infectious waste destruction and for irradiating cell membranes in biological materials to momentarily raise the temperature within the cell membranes to above several thousand degrees, causing cell membrane failure, and creating greater exposure of cell contents to oxidizing species in the anolyte.
 78. The apparatus of claim 53, further comprising use of ultrasonic energy, via the ultrasonic energy source communicating with the anolyte for inducing microscopic bubble implosions to affect a reduction in size of the individual second phase waste volumes dispersed in the anolyte.
 79. The apparatus of claim 53, further comprising an anolyte reaction chamber holding most of the anolyte portion and a foraminous basket, a penetrator attached to the basket to puncture solids increasing the exposed area, and further comprising an external CO₂ vent connected to the reaction chamber for releasing CO₂ into the atmosphere, a hinged lid attached to the reaction chamber allowing insertion of infectious waste into the anolyte portion as liquid, solid, or mixtures of liquids and solids, an anolyte pump connected to the reaction chamber, an inorganic compounds removal and treatment system connected to the anolyte pump for removing chlorides, and other precipitate forming anions present in the infectious waste being processed, thereby precluding formation of unstable oxycompounds.
 80. The apparatus of claim 79, further comprising an off-gas cleaning system, comprising scrubber/absorption columns connected to the vent, a condenser connected to the anolyte reaction chamber, whereby non-condensable incomplete oxidation products, low molecular weight organics and carbon monoxide are reduced to acceptable levels for atmospheric release by the gas cleaning system, and wherein the anolyte off-gas is contacted in the gas cleaning system wherein the noncondensibles from the condenser are introduced into the lower portion of the gas cleaning system through a flow distribution system and a small side stream of freshly oxidized anolyte direct from the electrochemical cell is introduced into the upper portion of the column, resulting in a gas phase continuously reacting with the oxidizing mediator species as it rises up the column past the down flowing anolyte, and external drain, for draining to an organic compound removal system and the inorganic compounds removal and treatment system, and for draining the anolyte system, wherein the organic compounds recovery system is used to recover biological materials that are benign and do not need further treatment, and biological materials that will be used in the form they have been reduced.
 81. The apparatus of claim 79, further comprising thermal control units connected to heat or cool the anolyte to a selected temperature range when anolyte is circulated into the reaction chamber through the electrochemical cell by pump on the anode chamber side of the membrane, a flush for flushing the anolyte, and a filter is located at the base of the reaction chamber to limit the size of exiting solid particles to approximately 1 mm in diameter.
 82. The apparatus of claim 53, wherein the direct current for the electrochemical cell is provided by a DC power supply, which is powered by an AC power supply, and wherein the DC power supply is low voltage high current supply operating at or below 10V DC and the AC power supply operates off an about 110v AC line for the smaller units and about 240v AC for larger units.
 83. The apparatus of claim 53, further comprising an electrolyte containment boundary composed of infectious waste materials resistant to the oxidizing electrolyte selected from a group consisting of stainless steel, PTFE, PTFE lined tubing, glass and ceramics, and combinations thereof.
 84. The apparatus of claim 53, further comprising an anolyte recovery system connected to a catholyte pump, a catholyte reservoir connected to the cathode portion of the electrochemical cell, a thermal control unit connected to the catholyte reservoir for varying the temperature of the catholyte portion, a bulk of the catholyte portion being resident in a catholyte reservoir, wherein the catholyte portion of the electrolyte flows into a catholyte reservoir, and further comprising an air sparge connected to the catholyte reservoir for introducing air into the catholyte reservoir.
 85. The apparatus of claim 84, further comprising an anolyte recovery system for capturing the anions and for reintroducing the anions into the anolyte chamber upon collection from the catholyte electrolyte, an off-gas cleaning system connected to the catholyte reservoir for cleaning gases before release into the atmosphere, and an atmospheric vent connected to the off-gas cleaning system for releasing gases into the atmosphere, wherein cleaned gas from the off-gas cleaning system is combined with unreacted components of the air introduced into the system and discharged through the atmospheric vent
 47. 86. The apparatus of claim 84, further comprising a screwed top on the catholyte reservoir to facilitate flushing out the catholyte reservoir, a mixer connected to the catholyte reservoir for stirring the catholyte, a catholyte pump connected to the catholyte reservoir for circulating catholyte back to the electrochemical cell, a drain for draining catholyte, a flush for flushing the catholyte system, and an air sparge connected to the housing for introducing air into the catholyte reservoir, wherein the catholyte portion of the electrolyte is circulated by pump through the electrochemical cell on the cathode side of the membrane, and wherein contact of oxidizing gas with the catholyte portion of the electrolyte is enhanced by promoting gas/liquid contact by mechanical and/or ultrasonic mixing.
 87. The apparatus of claim 53, wherein the electrochemical cell is operated at high membrane current densities above about 0.5 amps/cm² for increasing a rate of infectious waste destruction, also results in increased mediator ion transport through the membrane into the catholyte, and further comprising an anolyte recovery system positioned on the catholyte side, air sparging on the catholyte side to dilute and remove off-gas and hydrogen, wherein some mediator oxidizer ions cross the membrane and are removed through the anolyte recovery system to maintain process efficiency or cell operability.
 88. The apparatus of claim 53, further comprising a controller, a microprocessor, a monitor and a keyboard connected to the cell for inputting commands to the controller through the keyboard responding to the information displayed on the monitor, a program in the controller sequencing the steps for operation of the apparatus, program having pre-programmed sequences of operations the operator follows or chooses other sequences of operations, the controller allows the operator to select sequences within limits that assure a safe and reliable operation, the controller sends digital commands that regulate electrical power to pumps, mixers, thermal controls, ultraviolet sources, ultrasonic sources, CO₂ vents, air sparge, and the electrochemical cell, the controller receives component response and status from the components, the controller sends digital commands to the sensors to access sensor information through sensor responses, sensors in the apparatus provide digital information on the state of components, sensors measure flow rate, temperature, pH, CO₂ venting, degree of oxidation, and air sparging, the controller receives status information on electrical potential across the electrochemical cell or individual cells in a multi-cell configuration and between the anodes and reference electrodes internal to the cells and the current flowing between the electrodes within each cell.
 89. A infectious waste destruction system, comprising a housing constructed of metal or high strength plastic surrounding an electrochemical cell, with electrolyte and a foraminous basket, an AC power supply with a power cord, a DC power supply connected to the AC power supply, the DC power supply providing direct current to the electrochemical cell, a control keyboard for input of commands and data, a monitor screen to display the systems operation and functions, an anolyte reaction chamber with a basket, status lights for displaying information about the status of the treatment of the infectious waste material, an air sparge for introducing air into a catholyte reservoir below a surface of a catholyte, a CO₂ vent incorporated into the housing to allow for CO₂ release from the anolyte reaction chamber, an atmospheric vent facilitating the releases of gases into the atmosphere from the catholyte reservoir, a hinged lid for opening and depositing the infectious waste in the basket in the anolyte reaction chamber, a locking latch connected to the hinged lid, and in the anolyte reaction chamber an aqueous acid, alkali, or neutral salt electrolyte and mediated oxidizer species solution in which an oxidizer form of a mediator redox couple initially may be present or may be generated electrochemically after introduction of the infectious waste and application of DC power to the electrochemical cell.
 90. The system of claim 89, wherein the infectious waste is introduced when the anolyte is at room temperature, operating temperature or intermediate temperature, and the infectious waste material is rapidly oxidized at temperatures below boiling point of anolyte at ambient pressure, and further comprising a pump circulating an anolyte portion of an electrolyte, an in-line filter preventing solid particles large enough to clog electrochemical cell flow paths from exiting the reaction chamber, an inorganic compound removal and treatment system and drain outlets connected to the anolyte reaction chamber, whereby residue is pacified in the form of a salt and may be periodically removed, and a removable top connected to a catholyte reservoir allowing access to the reservoir for cleaning and maintenance.
 91. A infectious waste oxidizing process, comprising an operator engaging an ‘ON’ button on a control keyboard, a system controller which contains a microprocessor, running a program and controlling a sequence of operations, a monitor screen displaying process steps in proper sequence, status lights on the panel providing status of the process, opening a lid and placing the infectious waste in a basket as a liquid, solid, or a mixture of liquids and solids, retaining a solid portion of the infectious waste and flowing a liquid portion through the basket and into an anolyte reaction chamber, activating a locking latch after the infectious waste is placed in the basket, activating pumps which begins circulating the anolyte and a catholyte, once the circulating is established throughout the system, operating mixers, once flow is established, turning on thermal control units, and initiating anodic oxidation and electrolyte heating programs, energizing an electrochemical cell to electric potential and current density determined by the controller program, using programmed electrical power and electrolyte temperature ramps for maintaining a predetermined infectious waste destruction rate profile as a relatively coolant reaction rate as more reactive infectious waste components are oxidized, thus resulting in the remaining infectious waste becoming less and less reactive, thereby requiring more and more vigorous oxidizing conditions, activating ultrasonic and ultraviolet systems in the anolyte reaction chamber and catholyte reservoir, releasing CO₂, from the infectious waste oxidizing process in the anolyte reaction chamber, activating air sparge and atmospheric vent in a catholyte system, monitoring progress of the process in the controller by cell voltages and currents, monitoring CO₂, CO, and O₂ gas composition for CO₂, CO and oxygen content, decomposing the infectious waste into water and CO₂, the latter being discharged out of the CO₂ vent, air sparging drawing air into a catholyte reservoir, and discharging excess air out of an atmospheric vent, determining with an oxidation sensor that desired degree of infectious waste destruction has been obtained, setting the system to standby, and executing system shutdown using the controller keyboard system operator.
 92. The process of claim 91, further comprising placing the system in a standby mode during the day and adding infectious waste as it is generated throughout the day, placing the system in full activation during non-business hours, operating the system at low temperature and ambient atmospheric pressure and not generating toxic compounds during the destruction of the infectious waste, making the process indoors compatible, scaling the system between units small enough for use by a single practitioner and units large enough to replace hospital incinerators, releasing CO₂ oxidation product from the anolyte system out through the CO₂ vent, and venting off-gas products from the catholyte reservoir through the atmospheric vent.
 93. The process of claim 91, further comprising introducing the infectious waste into a room temperature or cooler system with little or none of the mediator redox couple in the oxidizer form, depending upon reaction kinetics, heat of reaction and similar infectious waste characteristics. 